JP2018530692A - Conversion of waste heat from gas processing plant to electricity and cooling based on organic Rankine cycle - Google Patents

Abstract

The system includes a waste heat recovery heat exchanger that heats a heating fluid stream in exchange with a heat source in a crude oil gas treatment plant and an organic Rankine cycle energy conversion system. The conversion system includes: And a cooling subsystem that includes one or more cooling elements that cool one or more of the process streams and the cooling water stream for cooling the outside air. The conversion system generates power upon expansion of an ejector that receives a second portion of the working fluid from the cooling subsystem, a third portion of the working fluid, and a fourth portion of the working fluid. And a cooling element that cools the working fluid stream including the working fluid output stream from the ejector and the expanded fourth portion of the working fluid from the turbine and generator.
[Selection] Figure 7A

Description

  This application claims priority from US Patent Application No. 62 / 209,147 filed on August 24, 2015 and US Patent Application No. 14 / 978,359 filed on December 22, 2015. The contents of the US patent application are incorporated herein by reference.

  Natural gas and crude oil may be found in a common reservoir. In some cases, a gas processing plant can purify untreated natural gas by removing common impurities, such as water, carbon dioxide, and hydrogen sulfide. Some materials that impure natural gas have economic value and can be further processed, sold, or processed and sold. Crude oil associated gas processing plants often release large amounts of waste heat to the environment.

  In one aspect, the system includes a waste heat recovery heat exchanger configured to heat the heating fluid stream by exchange with a heat source in a crude oil associated gas processing plant; and an organic Rankine cycle energy conversion system. The organic Rankine cycle energy conversion system includes an energy conversion heat exchanger configured to heat a first portion of a working fluid comprising isobutane by exchange with a heated heating fluid stream. The organic Rankine cycle energy conversion system is configured to cool one or more of a process stream from a crude oil gas treatment plant and a cooling water stream for ambient air cooling by replacement with a second portion of the working fluid. A cooling subsystem including one or more configured cooling elements. The organic Rankine cycle energy conversion system includes a second portion of the working fluid from the cooling subsystem, and a third portion of the working fluid that is part of the heated first portion of the working fluid; Including an ejector that accepts An organic Rankine cycle energy conversion system includes a turbine and a generator configured to generate power by expansion of a fourth portion of a working fluid that is part of a heated first portion of the working fluid. including. The organic Rankine cycle energy conversion system is configured to cool a stream of working fluid that includes an output stream of working fluid from an ejector and an expanded fourth portion of working fluid from a turbine and a generator. Cooling elements included.

  Embodiments can include one or more of the following features.

  The working fluid stream output from the cooling element is divided into the first portion of working fluid and the second portion of working fluid.

  The ejector geometry is: (i) the ratio of the amount of working fluid in the first part of the working fluid to the amount of working fluid in the second part of the working fluid; and (ii) the working Determined based on one or more of the ratio of the amount of working fluid in the third portion of fluid to the amount of working fluid in the fourth portion of working fluid.

  The ratio of the amount of working fluid in the first portion of working fluid to the amount of working fluid in the second portion of working fluid is between about 0.90 and about 0.92, The ratio of the amount of working fluid in the third portion of working fluid to the amount of working fluid in the fourth portion of working fluid is between about 0.27 and about 0.38. The ejector entrainment ratio is 3.5. The ratio of the cross-sectional area of the fixed area section of the ejector to the cross-sectional area of the throat portion (narrowest portion) of the ejector nozzle is about 6.4. The ratio of the cross-sectional area of the ejector low-pressure opening to the cross-sectional area of the ejector nozzle throat is about 2.9.

  The temperature of the second portion of the working fluid is between 45 ° F. (about 7.22 ° C.) and 55 ° F. (about 12.8 ° C.) when entering the cooling subsystem, On exit, it is between 75 ° F (about 23.9 ° C) and 85 ° F (about 29.4 ° C).

  The cooling subsystem includes at least one first cooling element configured to cool a process stream from a crude oil associated gas processing plant; and at least one configured to cool a cooling water stream for external air cooling. Two second cooling elements.

  The ratio of the volume of working fluid flowing through the at least one first cooling element to the volume of working fluid flowing through the at least one second cooling element is adjustable.

  The energy conversion heat exchanger is configured to heat the first portion of the working fluid to a temperature between 150 ° F. (about 65.6 ° C.) and 160 ° F. (about 71.1 ° C.). Yes.

  The system includes a plurality of ejectors connected in parallel.

  The cooling subsystem is configured to produce a cooling capacity between 60 MW (megawatts) and 85 MW. The turbine and generator are configured to generate power between 30 MW and 60 MW.

  The system includes a pump configured to increase the first portion of the working fluid to a pressure between 11 bar (1.1 MPa) and 12 bar (1.2 MPa).

  A cooling element moves the working fluid from a temperature between 110 ° F (about 43.3 ° C) and 120 ° F (about 48.9 ° C) to 80 ° F (about 65.6 ° C) and 90 ° F. It is configured to cool to a temperature between (about 65.6 ° C.).

  The system includes a storage tank, and the heating fluid flows from the storage tank through the waste heat recovery heat exchanger, through the organic Rankine cycle energy conversion system, and back to the storage tank.

  The waste heat recovery heat exchanger is configured to heat the heating fluid stream by exchange with a steam stream from a slag catcher in the inlet region of the gas processing plant. The waste heat recovery heat exchanger is configured to heat the heating fluid stream by exchange with an output stream from a diglycolamine (DGA) stripper in a gas processing plant. The waste heat recovery heat exchanger is configured to heat the heating fluid stream by exchange with one or more of a sweet gas stream and a sales gas stream in the gas processing plant. The waste heat recovery heat exchanger is configured to heat the heating fluid stream by replacement with a propane header in a propane refrigeration unit of the gas processing plant in the gas processing plant.

  In one aspect, the method comprises heating a heating fluid stream by exchange with a heat source in a crude oil associated gas processing plant via a waste heat recovery heat exchanger; and power and cooling capabilities in an organic Rankine cycle energy conversion system Generating. The step of generating electrical power and cooling capacity in the organic Rankine cycle energy conversion system comprises converting a first portion of the working fluid comprising isobutane by exchange with a heated heating fluid stream via an energy conversion heat exchanger. Heating; cooling one or more of the process stream from the crude oil associated gas processing plant and the cooling water stream for cooling the outside air by exchanging with a second portion of the working fluid in the cooling subsystem; Mixing in the ejector a second portion of the working fluid from the cooling subsystem and a third portion of the working fluid that is part of the heated first portion of the working fluid. A fourth part of the working fluid that is part of the heated first portion of the working fluid in the turbine and generator Generating electrical power by expansion of; and cooling a stream of working fluid comprising: an output stream of working fluid from the ejector; and an expanded fourth portion of working fluid from the turbine and generator Steps.

  Embodiments can include one or more of the following features.

  The method includes dividing a working fluid stream output from the cooling element into a first portion of working fluid and a second portion of working fluid.

  The method includes (i) a ratio of the amount of working fluid in the first portion of working fluid to the amount of working fluid in the second portion of working fluid; and (ii) a third of working fluid. Adjusting one or more of the ratios of the amount of working fluid in the portion and the amount of working fluid in the fourth portion of the working fluid. The method includes adjusting one or more of the ratios based on the target cooling capacity. The method includes connecting an ejector to an organic Rankine cycle energy conversion system, the ejector being selected based on one or more of the ratios.

  Cooling one or more of the process stream and the coolant stream in the cooling subsystem includes producing a cooling capacity between 60 MW and 85 MW.

  The step of generating power includes the step of generating power between 40 MW and 60 MW.

  The method includes boosting a first portion of the working fluid to a pressure between 11 bar (1.1 MPa) and 12 bar (1.2 MPa).

  The method includes flowing a heating fluid stream from the storage tank, through the waste heat recovery heat exchanger, through the organic Rankine cycle energy conversion system, and back to the storage tank.

  In one aspect, the system comprises a waste heat recovery heat exchanger configured to heat a heating fluid stream by exchange with a heat source in a crude oil gas treatment plant; and by exchange with a heated heating fluid stream An energy conversion system heat exchanger configured to heat the working fluid; and an energy conversion system including a turbine and a generator, wherein the turbine and the generator generate power by expansion of the heated working fluid It is configured as follows.

  Embodiments can include one or more of the following features.

  This energy conversion system includes an organic Rankine cycle. The turbine and generator are configured to generate at least about 65 MW (megawatts) of power, for example at least about 80 MW of power. The energy conversion system includes a pump configured to pressurize the energy conversion fluid to a pressure of less than about 12 bar (1.2 MPa). The working fluid includes isobutane.

  This energy conversion system includes a carina cycle. The working fluid includes ammonia and water. The turbine and generator are configured to generate at least about 65 MW of power, such as at least about 84 MW of power. The energy conversion system includes a pump configured to pressurize the working fluid to a pressure of less than about 25 bar (2.5 MPa), such as less than about 22 bar (2.2 MPa).

  This energy conversion system includes an improved Goswami cycle. This improved Goswami cycle includes a chiller that cools the cryogenic fluid stream. A first portion of the working fluid enters the turbine and a second portion of the working fluid flows through the chiller. The chiller is configured to cool the cryogenic fluid stream by replacement with a second portion of the working fluid. The cooled cryogenic fluid stream is used for cooling in a gas processing plant. The chiller is configured to produce an in-plant cooling capacity of at least about 210 MMBtu / hour (million British thermal units (Btu) per hour) (about 221562 MJ / h (MW)). The cooled cryogenic fluid stream is used to cool the outside air. The cooled cryogenic fluid stream is used for outside air cooling in the gas processing plant. The chiller is configured to produce an outdoor air cooling capacity of at least about 80 MMBtu / hour (about 84405 MJ / h (MW)). The cooled cryogenic fluid stream is used to cool the outside air of the community outside the gas processing plant. The chiller is configured to produce an outdoor air cooling capacity of at least about 1300 MMBtu / hour (about 1371573 MJ / h (MW)). The ratio of the amount of working fluid flowing through the turbine to the amount of working fluid flowing through the chiller can be adjusted during operation of the energy conversion system. The ratio can be zero. The turbine and generator are configured to generate at least about 53 MW of power. The energy conversion system includes a pump configured to pressurize the working fluid to a pressure of less than about 14 bar (1.4 MPa). The working fluid includes ammonia and water. The working fluid enters the turbine in the gas phase. The working fluid entering the turbine is ammonia rich compared to the working fluid in other parts of the energy conversion cycle. The system includes a high pressure recovery turbine configured to generate electrical power from a liquid working fluid. The high pressure recovery turbine is configured to generate at least about 1 MW of power. The liquid working fluid entering this high pressure recovery turbine is ammonia lean compared to the working fluid in the other parts of the energy conversion cycle.

  The heating fluid stream contains oil. The system includes a storage tank. The heating fluid stream flows from the storage tank through the waste heat recovery heat exchanger, through the energy conversion system heat exchanger, and back to the storage tank.

  The waste heat recovery heat exchanger is configured to heat the heating fluid stream by exchange with a vapor stream from a slag catcher at the inlet region of the gas processing plant. The waste heat recovery heat exchanger is configured to heat the heating fluid stream by exchange with a lean DGA stream from a diglycolamine (DGA) stripper in a gas processing plant. The waste heat recovery heat exchanger is configured to heat the heating fluid stream by exchange with the overhead stream from the DGA stripper at the gas processing plant. The waste heat recovery heat exchanger is configured to heat the heating fluid stream by exchange with a sweet gas stream in a gas processing plant. The waste heat recovery heat exchanger is configured to heat the heating fluid stream by exchange with a sales gas stream in a gas processing plant. The waste heat recovery heat exchanger is configured to heat the heating fluid stream by replacement with a propane header of a propane refrigeration unit of the gas processing plant in the gas processing plant.

  In a general aspect, the method comprises heating a heating fluid stream by exchange with a heat source in a gas processing plant; heating a working fluid by exchange with a heated heating fluid stream; Generating power by a turbine and a generator in the energy conversion system by expansion of the working fluid.

  Embodiments can include one or more of the following features.

  This energy conversion system includes an organic Rankine cycle. Generating the power includes generating at least about 65 MW of power, such as at least about 80 MW of power. The method includes applying a pressure of less than about 12 bar to the working fluid.

  This energy conversion system includes a carina cycle. Generating the power includes generating at least about 65 MW of power, eg, at least about 84 MW of power. The method includes applying a pressure of less than about 25 bar to the working fluid, such as a pressure of less than about 22 bar.

  The energy conversion cycle includes an improved Goswami cycle. The method includes the step of cooling the cryogenic fluid stream by exchange with working fluid in a chiller. A first portion of the working fluid enters the turbine and a second portion of the working fluid flows through the chiller. The method includes providing a cooled cryogenic fluid stream to a gas processing plant for cooling. The method includes producing in-plant cooling of at least about 210 MMBtu / hour using a cooled cryogenic fluid stream. The method includes using a cooled cryogenic fluid stream for external air cooling. The method includes using the cooled cryogenic fluid stream for outside air cooling in a gas processing plant. The method includes producing an outdoor air cooling capacity of at least about 80 MMBtu / hour. The method includes using the cooled cryogenic fluid stream for outside air cooling of a community outside the gas processing plant. The method includes producing an outside air cooling capacity of at least about 1300 MMBtu / hour. The method includes adjusting a ratio between the amount of working fluid entering the turbine and the amount of working fluid flowing through the chiller. This ratio can also be zero. Generating power includes generating at least about 53 MW of power. The method includes pressurizing the working fluid to a pressure less than about 14 bar. The method includes allowing the working fluid to enter the turbine in the gas phase. The working fluid entering the turbine is ammonia rich compared to the working fluid in other parts of the energy conversion cycle. The method includes generating power by a high pressure recovery turbine that receives a liquid working fluid. The method includes generating at least about 1 MW of power. The liquid working fluid received in the high pressure recovery turbine is ammonia lean compared to the working fluid in the other parts of the energy conversion cycle.

  This method converts a heating fluid stream from a storage tank for exchange with a heat source in a gas processing plant to a waste heat recovery exchanger in the gas processing plant and to an energy conversion heat exchanger for exchange with an energy conversion fluid. Flushing and returning to the accumulation tank.

  The method includes heating a heating fluid stream by exchange with a steam stream from a slag catcher in an inlet region of a gas processing plant. The method includes heating the heating fluid stream by exchange with a lean DGA stream from a DGA stripper in a gas processing plant. The method includes heating the heating fluid stream by exchange with a top stream from a DGA stripper in a gas processing plant. The method includes heating the heating fluid stream by exchange with a sweet gas stream in a gas processing plant. The method includes heating the heating fluid stream by exchange with a sales gas stream in a gas processing plant. The method includes heating the heating fluid stream by replacement with a propane header in a propane refrigeration unit of the gas processing plant in the gas processing plant.

  The system described herein has one or more of the following advantages. The system can be integrated with a crude oil associated gas processing plant to increase the energy efficiency of the gas processing plant, reduce pollution, or both. Low-grade waste heat from gas processing plants can be used for carbon-free power generation. Low-grade waste heat from the gas processing plant can be used to provide near-outside air cooling within the plant, thus reducing fuel consumption in the gas processing plant. The low-grade waste heat from the gas processing plant can be used to provide air conditioning or cooling of outside air in the industrial community of the gas processing plant or nearby non-industrial communities, thus helping to reduce the energy consumption of the community.

  The described energy conversion system can be integrated as an improvement into an existing crude oil gas processing plant or can be integrated into a new gas processing plant. Improvements to existing gas processing plants allow the benefits of efficiency, power generation and fuel saving provided by the energy conversion system described herein to be enjoyed with less capital investment. The energy conversion system can utilize existing structures in a gas processing plant while allowing efficient waste heat recovery and conversion of waste heat into power generation and cooling utilities. The introduction of an energy conversion system into an existing gas processing plant can be generalized for operation modes specific to the plant.

  Other features and advantages will be apparent from the following description and the claims.

It is a figure of the entrance area | region of a crude oil accompanying gas processing plant.

It is a figure of the high-pressure gas processing area | region of a crude oil accompanying gas processing plant.

1 is a diagram of a low pressure gas treatment and feed gas compression section of a crude oil associated gas treatment plant. FIG.

1 is a diagram of a liquid recovery and sales gas compression unit of a crude oil-associated gas processing plant.

FIG. 3 is a diagram of a propane refrigerant compartment of a crude oil associated gas processing plant.

1 is a diagram of a waste heat power conversion plant based on an organic Rankine cycle. FIG.

1 is a diagram of a combined waste heat cooling and power conversion plant based on an organic Rankine cycle. 1 is a diagram of a combined waste heat cooling and power conversion plant based on an organic Rankine cycle.

It is a figure of an ejector.

1 is a diagram of a waste heat power conversion plant based on an improved carina cycle. FIG. 1 is a diagram of a waste heat power conversion plant based on an improved carina cycle. FIG.

1 is a diagram of a combined waste heat cooling and power conversion plant based on an improved Goswami cycle. FIG. 1 is a diagram of a combined waste heat cooling and power conversion plant based on an improved Goswami cycle. FIG.

1 is a diagram of a combined waste heat cooling and power conversion plant based on an improved Goswami cycle. FIG. 1 is a diagram of a combined waste heat cooling and power conversion plant based on an improved Goswami cycle. FIG.

1 is a diagram of a combined waste heat cooling and power conversion plant based on an improved Goswami cycle. FIG.

  The low-grade waste heat recovery network is integrated in the crude oil-associated gas processing plant. The low grade waste heat recovery network can include a network of heat exchangers in the gas processing plant that recover waste heat from various low quality sources in the gas processing plant. The recovered waste heat can be sent to an energy conversion system, such as an energy conversion system based on an organic Rankine cycle, a carina cycle, or an improved Goswami cycle.

  In the energy conversion system, the recovered waste heat can be used for conversion to carbon-free power. Depending on the type of energy conversion system, the recovered waste heat is used for cooling the low-temperature water, and this low-temperature water is then returned to the treatment plant for use in quasi-outside air temperature reduction in the plant, or Used to directly cool a gas stream in a gas processing plant. Thus, the dependence of the gas processing plant on mechanical refrigeration or propane refrigeration is reduced and energy efficiency is increased. In some types of energy conversion systems, the recovered waste heat may be used to provide outdoor air conditioning or cooling to the industrial community of the gas processing plant or nearby non-industrial communities. The amount of waste heat used for power generation relative to the amount of waste heat used for cooling is flexible in real time so that the operation of the energy conversion system can be optimized based on the actual situation, for example, environmental conditions and demand from the power grid. Can be adjusted. For example, during a hot summer day, the energy conversion system may be configured to provide mainly outdoor air conditioning at the expense of power generation, and in the winter, the energy conversion system may be configured to increase power generation. May be.

  FIGS. 1-5 illustrate a portion of a large crude oil associated gas processing plant having a supply capacity of, for example, about 2 to 2.5 billion standard cubic feet per day. In some cases, a gas processing plant is a plant for processing “associated gas”, which is gas associated with crude oil obtained from an oil well, or “natural gas”, which is gas obtained directly from a natural gas well. It is a plant for.

  A low-grade waste heat recovery network and a semi-outside air cooling system are integrated into the crude oil associated gas treatment plant of FIGS. 1-5 as an improvement to the crude gas treatment plant. A network of heat exchangers integrated in a crude oil-associated gas processing plant recovers waste heat from various low-grade sources in the gas processing plant. The recovered waste heat is sent to an energy conversion system where the recovered waste heat is converted to carbon-free power. In the energy conversion system, the recovered waste heat can be used to cool the low-temperature water returned to the gas processing plant for lowering the temperature outside the plant, thereby reducing the energy consumption used by the gas processing plant for cooling. It can also be reduced. In some cases, the recovered waste heat can be used to provide outside air conditioning or cooling to the industrial community of the gas processing plant or to nearby non-industrial communities.

  Prior to the improved introduction of the low-grade waste heat recovery network and quasi-outside air cooling system described herein, crude oil-associated gas processing plants such as those shown in FIGS. 232 ° F. (waste heat less than about 111 ° C.) was discarded to the environment. As an example, such a plant is disposing of low grade waste heat of about 3250 MMBtu / hour (about 3428932 MJ / h (MW)) to the environment. In addition, such plants consumed about 500 MMBtu / hour (about 527528 MJ / h (MW)) for semi-outside air cooling to operate the liquid recovery area 400 (FIG. 4) prior to the introduction of the improvements. . By introducing the low-grade waste heat recovery network and the semi-outside air cooling system described here, the amount of low-grade waste heat released to the environment can be reduced, and the semi-outside air cooling load accompanying the operation of the liquid recovery area can be reduced.

  In operation, the heating fluid is flowed through heat exchangers 1 to 7 (described in the following paragraphs). The inlet temperature of the heating fluid flowing into each inlet of heat exchangers 1 to 7 is substantially the same, for example, about 130 ° F. (about 54.4 ° C.) and about 150 ° F. (about 65.6 ° C.). Temperature), for example, about 140 ° F. (about 60 ° C.), about 150 ° F., about 160 ° F. (about 71.1 ° C.), or another temperature. Each heat exchanger 1 to 7 heats the heating fluid to a respective temperature higher than the inlet temperature. The heated heating fluids from heat exchangers 1 to 7 merge and flow through the power generation system, where heat from the heated heating fluid heats the power generation system working fluid, The pressure and temperature of the working fluid increases.

  Referring to FIG. 1, in an inlet region 100 of a crude oil associated gas processing plant, an inlet gas stream 102, for example, a three-phase oil well fluid supply stream, flows to receiving slag catchers 104, 106. The slag catchers 104, 106 are first stage three-phase separators of oil well stream hydrocarbon (HC) condensate, gas, and sour water (concentrated waste).

  Well stream HC condensate 124, 126 from each slag catcher 104, 106 flows to three-phase separators 128, 129, respectively, for flushing and further separation. In the three-phase separators 128, 129, the gas is separated from the liquid, and the HC liquid is separated from the condensed water. The overhead gas 132, 134 flows to the low pressure (LP) gas separator 118. Sour water 136, 138 flows to the sour water stripper pre-flash drum 112. The HC condensate 140, 142 flows through the three-phase separator condensate cooler 144 and is pumped to the crude injection header 148 by one or more condensate pumps 146.

  Hot steam 114, 116 from the slag catchers 104, 106, respectively. The heat exchanger 1 recovers waste heat from the steam 114, 116 by exchange with a heating fluid 194, such as oil, water, organic fluid, or another fluid. For example, the heat exchanger 1 has a waste heat between about 50 MMBtu / hour (about 52753 MJ / h (MW)) and about 150 MMBtu / hour (about 158258 MJ / h (MW)), for example, about 50 MMBtu / hour, 100 MMBtu / hour (about 105506 MJ / h (MW)), about 150 MMBtu / hour, or another amount of waste heat can be recovered. The heat exchanger 1 changes the temperature of the heating fluid 194, for example, from the inlet temperature to a temperature between about 180 ° F. (about 82.2 ° C.) and about 200 ° F. (about 93.3 ° C.). E.g., about 180 [deg.] F., about 190 [deg.] F. (about 87.8 [deg.] C.), about 200 [deg.] F., or another temperature, while cooling the top vapors 114, 116 from the slag catchers 104, 106 To do. The heating fluid 194 leaving the heat exchanger 1 is sent to a heating fluid system header that carries the heated heating fluid to, for example, a power generation unit or a combined cooling and power generation plant.

  Following the waste heat recovery in the heat exchanger 1, the steams 114 and 116 are cooled by the slag catcher steam cooler 122. The operation of the steam cooler 122 can vary from season to season. For example, in the summer, the temperature of the incoming steam 114, 116 may be higher than in the winter, and the steam cooler 112 operates at a lower heat duty in the summer than in the winter, and in the summer than in the winter. The steam 114, 116 can be cooled to a high temperature. The presence of the heat exchanger 1 can reduce the heat duty of the cooler 122 as compared to the case where the heat exchanger 1 is not provided. For example, the thermal duty of the cooler 122 is, for example, between about 20 MMBtu / hour (about 21101 MJ / h (MW)) and about 40 MMBtu / hour (about 42202 MJ / h (MW)), for example, about 20 MMBtu / hour. Can be reduced to about 30 MMBtu / hour (about 311652 MJ / h (MW)), about 40 MMBtu / hour, or another thermal duty, but the heat duty of the cooler 122 without the heat exchanger 1 is About 120 MMBtu / hour (about 126607 MJ / h (MW)) and about 140 MMBtu / hour (about 147708 MJ / h (MW)) in summer, about 190 MMBtu / hour (about 20041 MJ / h (MW)) in winter And about 210 MMBtu / hour.

  The cooled sour gas output stream 180 from the slag catcher steam cooler 122 is divided into two parts. The first portion 130 of cooled sour gas flows to the high pressure gas processing section 200 (FIG. 2). The cooled second portion 123 of sour gas flows to the LP gas separators 118, 120 where all the entrained moisture of the steam 114, 116 is removed. Sour gases 150, 152 from the top of the LP gas separators 118, 120 flow through a demister pad (not shown) that provides additional protection against liquid entrainment and are sent to the low pressure gas processing section 300 (FIG. 3). It is done. The HC liquids 154 and 156 from the LP gas separators 118 and 120 are sent to the HC condensate surge drum injection header 158 or the unpurified injection header 148.

Each slag catcher 104, 106 has a water boot to settle entrained sediment that collects sour water containing salt before the sour water 108, 110 is sent to the sour water stripper pre-flush drum 112, respectively. In the pre-flush drum 112, the sour water is removed from the sour water by removing dissolved hydrogen sulfide (H ₂ S) and hydrocarbons from the sour water, and all the entrained oil is removed from the sour water. The The top acid gas 160 from the preflash drum 112 is sent to the sulfur recovery unit 162. The sour water 164 from the pre-flash drum 112 is fed into the top section of the sour water stripper tower 166. The sour water flows down through the packing section of the stripper column 166 where it contacts the low pressure steam 168 that is injected below the packing section of the stripper column 166. The steam 168 extracts H ₂ S from the sour water. H ₂ S 170 flows from the top of the stripper column 166 to the sulfur recovery unit 162. The H ₂ S free water 172 flows from the bottom of the stripper tower 166 through a sour water effluent cooler 174, eg, an air cooler, to the suction side of the sour water reflux pump 176. The reflux pump 176 discharges the reflux water and returns it to the stripper column 166 or sends it to a gas plant oil-mixed sewage system, such as an evaporation pond 178.

Referring to FIG. 2, the high pressure gas processing section 200 of the gas processing plant includes a gas processing region 202 and a dehydration unit 204. The high pressure gas processing section 200 processes the high pressure sour gas 130 received from the inlet section (FIG. 1) of the gas processing plant. The gas treatment region 202 treats the sour gas 130 using, for example, diglycolamine (DGA) to remove impurities such as hydrogen sulfide (H ₂ S) and carbon dioxide (CO ₂ ), and generates a wet sweet sales gas 250. To do. Sweet gas is a gas from which H ₂ S has been removed. Sweet gas may contain a small amount of H ₂ S in the gas stream, for example, less than about 10 PPM (parts per million) H ₂ S.

  The sour feed gas 130 can be cooled by one or more heat exchangers or chillers 206. For example, the chiller 206 can be an intermittent load chiller that cools the sour supply gas 130. From chiller 206, sour feed gas 130 flows to feed gas filter separator 208. A waste filter in the filter separator 208 removes solid particles such as mud or iron sulfide from the sour gas 130. The entrained liquid in the sour gas 130 is separated by the vane demister in the filter separator 208.

The filtered sour gas 131 exits the filter separator 208 and enters the bottom of the diglycolamine (DGA) contactor 210. The sour gas rises in the DGA contactor and comes into contact with the liquid, that is, the lean DGA from the lean DGA stream 232 (discussed in the following paragraph) flowing down the column of the DGA contactor 210. The lean DGA in the DGA contactor 210 absorbs H ₂ S and CO ₂ from the sour gas. The wet sweet sales gas 250 exits the top of the DGA contactor and enters the dehydration unit 204, discussed in the following paragraph. The rich DGA 214, which is a liquid DGA rich in H ₂ S and CO ₂ , exits the bottom of the DGA contactor 210 and flows into the rich DGA flash drum 216. The sales gas is a gas mainly composed of methane, and includes heavier gases such as a small amount of ethane and a very small amount of propane. Sales gas exhibits industrial and non-industrial heating values between about 900 and 1080 BTU / SCF (English thermal units per cubic foot).

  In the rich DGA flash drum 216, gas is separated from the liquid rich DGA. The gas is released as flash gas 218 from the top of the flash drum 216 and joins the fuel gas header 214 for use in, for example, a boiler.

Liquid rich DGA 220 exits the bottom of flash drum 216 and flows to DGA stripper 222 via lean / rich DGA cooler 219. The liquid rich DGA flows down the column of the DGA stripper 222 where it contacts acid gas and steam rising from the stripper bottom reboiler stream 224 through the column. Stripper bottom reboiler stream 224 is heated in exchanger 226 by exchange with low pressure steam (LPS) 228. H ₂ S and CO ₂ are released with the mixture of DGA and water, and the stripper bottom reboiler stream 224 returns to the DGA stripper 222 as a two-phase flow.

  The acid gas rises through a column of DGA stripper 222 and exits the top of DGA stripper 222 as an acid gas stream 230 that may contain condensed sour water. The acid gas stream 230 flows to the DGA stripper overhead condenser 238 and then to the DGA stripper recirculation drum 240 that separates the acid gas and sour water. The acid gas 242 rises and exits the top of the reflux drum 240, from which the acid gas 242 is directed, for example, to a sulfur recovery unit 162 or acid flare. The sour water (not shown) exits the bottom of the reflux drum 240 and is transported by a stripper reflux pump (not shown) to the top tray of the DGA stripper 222 and acts as a top reflux stream.

  The lean DGA solution 232 flows from the bottom of the DGA stripper 222 and is pumped by one or more DGA circulation pumps 234 through the lean / rich DGA cooler 219, the heat exchanger 2, and the lean DGA solution cooler 236. The heat exchanger 2 recovers waste heat by exchanging with the heating fluid 294. For example, the heat exchanger 2 has a waste heat between about 200 MMBtu / hour (about 2111011 MJ / h (MW)) and about 300 MMBtu / hour (about 316517 MJ / h (MW)), for example about 200 MMBtu / hour, about 250 MMBtu. / Hour (about 263764 MJ / h (MW)), about 300 MMBtu / hour, or another amount of waste heat can be recovered. The heat exchanger 2 changes the temperature of the heating fluid 294 from, for example, an inlet temperature to a temperature between about 210 ° F. (about 98.9 ° C.) and about 230 ° (about 110 ° C.) F, for example, about The lean DGA stream 232 is cooled while increasing to 210 ° F., about 220 ° F. (about 104 ° C.), about 230 ° F., or another temperature. The heating fluid 294 exiting the heat exchanger 2 is sent to a heating fluid system header that carries the heated heating fluid to, for example, a power generation unit or a combined cooling and power generation plant.

  Due to the presence of the heat exchanger 2, the thermal duty of the lean DGA cooler 236 can be reduced. For example, the thermal duty of the lean DGA cooler 236 may be, for example, between a previous value of about 250 MMBtu / hr and about 300 MMBtu / hr to about 30 MMBtu / hr and about 50 MMBtu / hr, for example about It can be reduced to 30 MMBtu / hour, about 40 MMBtu / hour, or about 50 MMBtu / hour, or another thermal duty.

  In the gas sweetening process, complex products may be formed by side reactions between lean DGA and impurities. Such side reactions can reduce the absorption process efficiency of lean DGA. In some cases, a regenerator (not shown) can be used to convert these complex products back into the DGA. The lean DGA stream containing the complex product is transferred from the DGA stripper 222 to a regenerator that heats the lean DGA stream using steam, eg, 250 psig steam, to convert the complex product to DGA. Can send. Lean DGA vapor exits the top of the regenerator and returns to the DGA stripper 222. The regenerated DGA flows from the bottom of the regenerator to the DGA regenerator storage tank. The regeneration temperature in the regenerator can be controlled using the side stream of the reflux water.

  In the dewatering zone 204, the wet sweet sales gas 250, the top product from the DGA contactor 210, is processed to remove water vapor from the gas stream. The wet sweet sales gas 250 enters the bottom of a triethylene glycol (TEG) contactor 252. The wet sweet sales gas 250 rises in the TEG contactor 252 and contacts the liquid, ie, the lean TEG stream 280 (discussed in the following paragraphs) flowing down the column of the TEG contactor 252. In some cases, a hygroscopic liquid other than TEG can be used. The lean TEG in the TEG contactor 252 removes water vapor from the sweet sales gas. Dry sweet sales gas 254 flows from the top of TEG contactor 252 to sales gas knockout (KO) drum 256. The tower top 258 from the sales gas KO drum 256 is sent to the gas grid 261.

  The rich TEG 259 flows from the bottom of the TEG contactor 252 to the rich TEG flash drum 260. The bottom 263 from the sales gas KO drum 256 also flows to the rich TEG flash drum 260. From the top of the flash drum 260, gas is released as flash gas 262 and merges into the fuel gas header 214 for use, for example, in a boiler.

  Liquid rich TEG 264 exits the bottom of flash drum 260 and flows to TEG stripper 268 via lean / rich TEG exchanger 266. In the TEG stripper 268, water vapor is extracted from the liquid rich TEG by warm steam generated by a TEG stripper reboiler (not shown). The top off-gas 270 flows from the top of the TEG stripper 268 through the top condenser 272 to the TEG stripper off-gas recirculation drum 274. A reflux drum 274 separates offgas from the condensate. The off-gas 276 exits the top of the recirculation drum 274 and joins the fuel gas header 214 for use, for example, in a boiler. A TEG stripper recirculation pump (not shown) pumps the condensate 278 from the bottom of the recirculation drum 274 to the unpurified injection header 148 and also pumps water (not shown) to the waste water stripper.

  The lean TEG 280 from the bottom of the TEG stripper 268 is pumped by one or more lean TEG circulation pumps 282 to the lean / rich TEG exchanger 266 and then to the lean TEG cooler 284, and then to the top of the TEG contactor 252. Returned to

  Referring to FIG. 3, the low pressure gas processing and supply gas compression section 300 of the gas processing plant includes a gas processing region 302 and a supply gas compression region 304. The gas processing and compression section 300 processes sour gas 150, 152 received from the inlet section 100 (FIG. 1) of the gas processing plant.

The gas processing region 302 processes sour gases 150, 152 (collectively referred to as sour gas supply streams 306) to remove impurities, such as H ₂ S and CO ₂ , to produce a sweet gas 350. Sour gas feed stream 306 flows into feed gas filter separator 308. A waste filter in the filter separator 308 removes solid particles, such as mud or iron sulfide, from the sour gas feed stream 306. A vane demister in the filter separator 308 separates the entrained liquid in the sour gas supply stream 306.

The filtered sour gas feed stream 307 exits the filter separator 308 and enters the bottom of the DGA contactor 310. Sour gas ascends in DGA contactor 310 and contacts lean DGA from lean DGA stream 332 (discussed in the following paragraphs) flowing down the DGA contactor column. The lean DGA in the DGA contactor 310 absorbs H ₂ S and CO ₂ from the sour gas. The sweet gas 350 exits the top of the DGA contactor 310 and enters the feed gas compression zone 304 discussed in the following paragraph. The rich DGA 314 exits the bottom of the DGA contactor 310 and flows into the rich DGA flash drum 316.

  The rich DGA flash drum 316 reduces the pressure of the rich DGA 314 to separate the gas from the liquid rich DGA. The gas is released as flash gas 318 from the top of the flash drum 316 and joins the fuel gas header 214 (FIG. 2) for use, for example, in a boiler.

The liquid rich DGA 320 exits the bottom of the flash drum 316 and flows to the DGA stripper 322 via a cooler (not shown). Liquid rich DGA flows down the column of DGA stripper 322 and comes into contact with acid gas and steam rising from the stripper bottom reboiler stream 324 through the column. Stripper bottom reboiler stream 324 is heated in exchanger 326 by exchange with low pressure steam (LPS) 328. H ₂ S and CO ₂ are released along with the DGA and water mixture, and the stripper bottom reboiler stream 324 returns to the DGA stripper 322 as a two-phase flow.

  The acid gas rises through a column of DGA stripper 322 and exits the top of DGA stripper 322 as an acid gas stream 330. The acid gas stream 330 may contain condensed sour water. The third waste heat recovery exchanger 5 cools the acid gas stream 330 from the DGA stripper 322. The heat exchanger 5 recovers waste heat by exchanging with the heating fluid 384. For example, the heat exchanger 5 has a waste heat between about 300 MMBtu / hour and about 400 MMBtu / hour (about 422202 MJ / h (MW)), for example, about 300 MMBtu / hour, about 350 MMBtu / hour (about 369270 MJ / h ( MW)), about 400 MMBtu / hour, or another amount of waste heat. The heat exchanger 5 changes the temperature of the heating fluid 384, for example, from the inlet temperature to a temperature between about 190 ° F and about 210 ° F, for example, about 190 ° F, about 200 ° F, about 210 °. The acid gas stream 330 is cooled while increasing to F, or another temperature. The heated heating fluid 384 is sent to a heating fluid system header that carries the heated heating fluid to, for example, a power generation unit or a cooled combined power plant.

  The presence of the heat exchanger 5 allows the DGA stripper overhead condenser 338 to be bypassed. In the absence of heat exchanger 5, DGA stripper overhead condenser 338 lowers the temperature of acid gas stream 330 and condenses water. The DGA stripper overhead condenser 338 has a thermal duty between about 300 MMBtu / hour and about 400 MMBtu / hour, for example, about 300 MMBtu / hour, about 350 MMBtu / hour, about 400 MMBtu / hour, or another thermal duty. be able to. However, if the acid gas stream 330 is cooled by the heat exchanger 5 and thereby saves the total heat duty of the DGA stripper overhead condenser 338, the DGA stripper overhead condenser 338 is not used (eg, DGA stripper tower 338). The thermal duty of the top condenser 338 is reduced to zero).

  The cooled acid gas stream 330 enters a DGA stripper reflux drum 340 that acts as a separator. The acid gas 342 rises and exits from the top of the reflux drum 340, from which the acid gas 342 is directed, for example, to a sulfur recovery unit 162 or acid flare. The sour water 344 exits the bottom of the reflux drum 340 and is transferred to the top tray of the DGA stripper 322 by the stripper reflux pump 346 and acts as the top reflux stream.

  The lean DGA solution 332 flows from the bottom of the DGA stripper 322 and is pumped through the waste heat recovery exchanger 4 that cools the lean DGA stream 332 from the DGA stripper 322 by one or more DGA circulation pumps 334. The heat exchanger 4 recovers waste heat by exchanging with the heating fluid 398. For example, the heat exchanger 4 has a waste heat between about 1200 MMBtu / hour (about 1266067 MJ / h (MW)) and about 1300 MMBtu / hour, for example, about 1200 MMBtu / hour, about 1250 MMBtu / hour (about 1318820 MJ / h ( MW)), about 1300 MMBtu / hour, or another amount of waste heat. The heat exchanger 4 changes the temperature of the heating fluid 398, for example, from the inlet temperature, for example, to a temperature between about 260 ° F. (about 127 ° C.) and about 280 ° F. (about 138 ° C.), for example, about The lean DGA stream 332 is cooled while increasing to 260 ° F., about 270 ° F. (about 132 ° C.), about 280 ° F., or another temperature. The heated heating fluid 398 is sent to a heating fluid system header that carries the heated heating fluid to, for example, a power generation unit or a combined cooling and power generation plant. The cooled lean DGA solution 332 is fed to the top of the DGA contactor 310.

  The presence of the heat exchanger 4 allows one or more lean DGA solution coolers 336 to be bypassed. In the absence of heat exchanger 4, the lean DGA solution 332 may have a thermal duty between about 1200 MMBtu / hour and about 1300 MMBtu / hour, such as about 1200 MMBtu / hour, about 1250 MMBtu / hour, about 1300 MMBtu / hour, or another Cooled by a lean DGA solution cooler 336 that can have a thermal duty. However, if the lean DGA solution 332 is cooled by the heat exchanger 4 so that the total heat duty of the lean DGA solution cooler 336 is saved, the lean DGA solution cooler 336 is not used (eg, the lean DGA solution cooler 336 Thermal duty is reduced to zero).

  In the gas sweetening process, complex products may be formed by side reactions between lean DGA and impurities. Such side reactions can reduce the absorption process efficiency of lean DGA. In some cases, a regenerator (not shown) can be used to convert these complex products back into the DGA. A lean DGA stream containing a complex product can be sent from the DGA stripper 322 to a regenerator that uses steam to heat the lean DGA stream to convert the complex product to DGA. Lean DGA vapor exits the top of the regenerator and returns to the DGA stripper 322. The regenerated DGA flows from the bottom of the regenerator to the DGA regenerator storage tank. The regeneration temperature in the regenerator can be controlled using the side stream of the reflux water.

  In the feed gas compression region 304, the sweet gas 350, which is the top product from the DGA contactor 310, is compressed and cooled. The sweet gas 350 flows from the DGA contactor 310 into a suction washer 352 that removes water that condenses in the piping between the gas treatment region 302 and the supply compressor suction washer 352. For example, the suction cleaner 352 can have a wire mesh demister pad for water removal. The liquid 356 collected in the suction cleaner 354 is returned to the DGA flash drum (not shown). Dry gas 358 exits the top of suction washer 354 and flows to the suction side of supply compressor 360, which can be, for example, a four-stage centrifugal compressor. In some cases, feed compressor 360 may have multiple feed gas compression trains. Discharge from each of the feed gas compression trains of feed compressor 360 merges into a single header 362.

  After the feed compressor 360, the header 362 is cooled by the waste heat recovery exchanger 3 and subsequently cooled by the cooler 364. The heat exchanger 3 recovers waste heat by exchanging with the heating fluid 394. For example, the heat exchanger 3 may generate waste heat between about 250 MMBtu / hour and about 350 MMBtu / hour, for example, about 250 MMBtu / hour, about 300 MMBtu / hour, about 350 MMBtu / hour, or another amount of waste heat. Can be recovered. The heat exchanger 3 changes the temperature of the heating fluid 394, for example, from the inlet temperature to a temperature between about 260 ° F. and about 280 ° F., for example, about 260 ° F., about 270 ° F., about While the temperature is raised to 280 ° F. or another temperature, the discharge gas of the header 362 is cooled. The heated heating fluid 394 is sent to a heating fluid system header that carries the heated heating fluid to, for example, a power generation unit or a combined cooling and power generation plant. The cooled header 362 flows to the refrigeration compartment in the liquid recovery unit 400 (FIG. 4).

  The presence of the heat exchanger 3 makes it possible to reduce the heat duty of the compressor after the cooler 364. For example, the thermal duty of the compressor after the cooler 364 is, for example, between about 20 MMBtu / hour and about 40 MMBtu / hour from the previous value of about 200 MMBtu / hour and about 400 MMBtu / hour. Thermal duty can be reduced to, for example, about 20 MMBtu / hour, about 30 MMBtu / hour, about 40 MMBtu / hour, or another thermal duty.

  FIG. 4 shows a liquid recovery and sales gas compression unit 400 in a gas processing plant that cools and compresses a header 362 (also referred to as supply gas 362) received from the low pressure gas processing and supply gas compression section 300. The liquid recovery and sales gas compression unit 400 includes a first chilling train 402, a second chilling train 404, a third chilling train 406, and a demethanizer section 408. The liquid recovery and sales gas compression unit 400 further includes a propane refrigerant compartment 500 (FIG. 5) and an ethane refrigerant compartment (not shown).

  The liquid recovery and sales gas compression unit 400 includes a cryogenic water network that includes water chillers 10, 12. The water chillers 10, 12 are located in the improved liquid recovery unit 490 using cryogenic water produced in a combined cooling and power generation plant (eg, as shown in FIGS. 10A-10B, 11A-11B, 12). Cool the supply gas. The temperature of the low temperature water supplied to the water chillers 10, 12 is, for example, a temperature between about 35 ° F. (about 1.67 ° C.) and about 45 ° (about 7.22 ° C.) F, for example about 35 ° F. ° F, about 40 ° F (about 4.44 ° C), about 45 ° F, or another temperature (these temperatures may be referred to as initial hot water temperatures). The water chillers 10 and 12 replace propane refrigeration or mechanical refrigeration used in the liquid recovery unit 400 (FIG. 4).

  The feed gas 362 from the low pressure gas treatment and feed gas compression section 300 enters a first chilling train 402 that cools the feed gas 362. Feed gas 362 flows through a first residue / feed exchanger 410 that cools feed gas 362 by exchange with high pressure residue gas 454 discussed in the following paragraphs. Supply gas 362 is further cooled by water chiller 10. The cooling duty of the water chiller 10 is, for example, a cooling duty between about 50 MMBtu / hour and about 150 MMBtu / hour, for example, about 50 MMBtu / hour, about 100 MMBtu / hour, about 150 MMBtu / hour, or another cooling duty. . The water chiller 10 sets the temperature of the cold water 482 to a temperature between about 90 ° F. (about 32.2 ° C.) and about 110 ° F. (about 43.3 ° C.), for example, from the initial low temperature water temperature, for example, The feed gas 362 is cooled while being raised to about 90 ° F., about 100 ° F. (about 37.8 ° C.), about 110 ° F., or another temperature.

  In the absence of water chiller 10, supply gas 362 can be further cooled in a first propane supply chiller that cools supply gas 362 by vaporizing propane refrigerant on the shell side of the first propane supply chiller. The thermal duty of the first propane feed chiller is, for example, a thermal duty between about 50 MMBtu / hour and about 150 MMBtu / hour, such as about 50 MMBtu / hour, about 100 MMBtu / hour, about 150 MMBtu / hour, or another heat. It can be a duty. However, if the feed gas 362 is cooled by the water chiller 10, thereby saving the total heat duty of the first propane feed chiller, the first propane feed chiller is not used.

  The feed gas 362 from the water chiller 10 flows through a first cryogenic separator 414 that separates the feed gas 362 into three phases: a hydrocarbon feed gas 416, a condensed hydrocarbon 418, and water 420. Water 420 flows into the separator boot and is sent to a process water recovery drum from which the water can be utilized in the gas treatment unit, for example as make-up water.

  Condensed hydrocarbon 418, also referred to as first cryogenic liquid 418, is pumped from first cryogenic separator 414 by one or more liquid dehydrator feed pumps 424. The first cryogenic liquid 418 is pumped through a demethanizer feed coalescer 426 to remove free water associated with the first cryogenic liquid 418, for example, to avoid damage to a downstream dehydrator. The removed water 428 flows to a condensate surge drum (not shown). The remaining first cryogenic liquid 419 is pumped to one or more liquid dehydrators 430, eg, a pair of liquid dehydrators. Drying in the liquid dehydrator 430 can be accomplished by passing the first cryogenic liquid 419 through the activated alumina bed in the other liquid dehydrator while regenerating one liquid dehydrator. Alumina has a strong affinity for water under the conditions of the first low-temperature liquid 419. When the alumina in the first liquid dehydrator is saturated, the first liquid dehydrator is taken off-line and regenerated while the first low-temperature liquid 419 is passed through the second liquid dehydrator. The dehydrated first cryogenic liquid 421 exits the liquid dehydrator 430 and is sent to the column 432 of the demethanizer tower.

  The hydrocarbon feed gas 416 from the first cryogenic separator 414 flows through a demister (not shown) to one or more feed gas dehydrators 434 for drying, such as three feed gas dehydrators. Two of the three gas dehydrators can be put into operation at any time while the third gas dehydrator is regenerating or waiting. Drying in the gas dehydrator 434 can be achieved by passing a hydrocarbon feed gas 416 through a molecular sieve bed. The sieve has a strong affinity for water under the conditions of the supply gas 416. When the sieve of one of the gas dehydrators is saturated, the gas dehydrator is taken off-line for regeneration, and the gas dehydrator that has been on standby until then is put into operation.

  The dehydrated supply gas 417 exits the supply gas dehydrator 434 and enters a second chilling train 404 that cools the supply gas. In the second low temperature train 404, the dehydrated supply gas 417 is cooled by the water chiller 12. The water chiller 12 cooling duty is, for example, a cooling duty between about 50 MMBtu / hour and about 150 MMBtu / hour, for example, about 50 MMBtu / hour, about 100 MMBtu / hour, about 150 MMBtu / hour, or another cooling duty. . The water chiller 12 sets the temperature of the cold water 484 to a temperature between about 55 ° F. (about 12.8 ° C.) and about 75 ° F. (about 23.9 ° C.), eg, from the initial low temperature water temperature, eg, The feed gas 416 is cooled while increasing to about 55 ° F., about 65 ° F. (about 18.3 ° C.), about 75 ° F., or another temperature. Heated cold water 482, 484 from water chillers 10, 12 returns to the combined cooling and power plant.

  The feed gas 417 cooled and dehydrated through the water chiller 12 enters the tube side of the demethanizer reboiler 436. The liquid 438 captured on the first tray of the demethanizer column 432 is pumped to the shell side of the demethanizer reboiler 436 by the demethanizer reboiler pump 441. The dehydrated supply gas 417 heats the liquid 438 in the demethanizer reboiler 436 and vaporizes at least a part of the liquid 438. The heated liquid 438 returns to the demethanizer column 432 via the trim reboiler 443. The dehydrated supply gas 417 is cooled by exchange with the liquid 438.

  In the absence of the water chiller 12, the dehydrated feed gas 417 is further cooled in the second propane feed chiller by replacement with low temperature propane. The second propane feed chiller has, for example, a thermal duty between about 50 MMBtu / hour and about 150 MMBtu / hour, such as about 50 MMBtu / hour, about 100 MMBtu / hour, about 150 MMBtu / hour, or another thermal duty. Can have. However, if the dehydrated feed gas 417 is cooled by the water chiller 12, thereby saving the total heat duty of the second propane feed chiller, the second propane feed chiller is not used.

  The cold dehydrated feed gas 417 is then sent to a second residual / feed gas exchanger 442 that cools the cold dehydrated feed gas 417 by exchange with the high pressure residual gas 454. The cooling medium 444 (eg, non-condensed gas) from the third residual / feed gas exchanger 446 discussed in the following paragraphs flows through the shell side of the second residual / feed gas exchanger 442 and is dehydrated. The temperature of the supply gas 417 is lowered. The dehydrated feed gas 417 then passes through a third propane feed chiller 448 that further cools the dehydrated feed gas 417 by exchange with low temperature propane.

  The dehydrated feed gas 417 and condensed hydrocarbon liquid from the third feed chiller 448 enter the second cryogenic separator 450. In the second low-temperature separator 450, the hydrocarbon liquid 452 (also referred to as the second low-temperature liquid 452) is separated from the supply gas 423. The second chilled liquid 452 is sent to the demethanizer column 432, for example, the tray 10 of the demethanizer column 432, with a reduced flow. Feed gas 423 flows to a third residual / feed gas exchanger 446 in the third cryogenic train 406.

  The third chilling train 406 cools the supply gas 423 in two stages. In the first stage, the feed gas 423 from the second cryogenic separator 450 enters the tube side of the third residual / feed gas exchanger 446. The third residual / supply gas exchanger 446 cools the supply gas 423 by exchanging with the high pressure residual gas 454 on the shell side of the third residual / supply gas exchanger.

  In the second stage of the third chilling train 406, the supply gas 423 passes through a final supply chiller 456 that lowers the temperature of the supply gas 23 using ethane refrigerant. The feed gas 423 condensed hydrocarbon liquid from the final feed chiller 456 enters the third cryogenic separator 458. The third low temperature separator 458 separates the hydrocarbon liquid 460 (also referred to as the third low temperature liquid 460) from the supply gas 454. The third chilled liquid 460 is fed into the column 432 of the demethanizer tower.

  The feed gas 454 from the third cryogenic separator 458, also referred to as high pressure residual gas 454, is used in the third residual / feed gas exchanger to cool the incoming dehydrated feed gas 417. , Itself is heated. The high pressure residual gas 454 flows through the second residual / feed gas exchanger 442 where the dehydrated feed gas 417 is cooled and the high pressure residual gas 454 is heated. The high pressure residual gas 454 then flows through the first residual / feed gas exchanger 410 where the feed gas 362 is cooled and the high pressure residual gas 454 is heated.

  The demethanizer section 408 removes methane from hydrocarbons condensed from the feed gas in the cryogenic trains 402, 404, 406. The demethanizer 432 receives four main feed streams. The first feed stream to the demethanizer tower 432, eg, the tray 4 of the demethanizer tower 432, contains the first cryogen 418 from the first cryogenerator 414. The first feed stream can include a minimum flow circulation from one or more demethanizer reboiler pumps. The second feed stream to the demethanizer tower 432, eg, the tray 10 of the demethanizer tower 432, contains the second cryogen 452 from the second cryogenerator 452. The third feed stream to the demethanizer tower 432, eg, the tray 19 of the demethanizer tower 432, contains the third cryogenized liquid 460 from the third cryogenerator 458. A fourth feed stream (not shown) to the demethanizer 432 includes an outlet from the propane surge drum 526 (FIG. 5), an outlet from the propane condenser, an outlet from the demethanizer bottom pump 462, and a minimum. Streams from flow lines, as well as surge exhaust lines from natural gas liquid (NGL) surge zones, can be included. The demethanizer tower bottom 468 is pumped to the NGL surge zone 470 by a demethanizer tower bottom pump 462.

  The overhead low pressure (LP) residual gas 464 from the demethanizer tower 432 flows from the top of the demethanizer tower 432 to the tube side of the ethane subcooler 466. The condensed ethane exiting the ethane surge drum (not shown) flows through the shell side of the ethane subcooler 466. In the ethane subcooler 466, the LP residual gas 464 recovers heat from the condensed ethane to raise the temperature while cooling the condensed ethane. The LP residual gas 464 exiting the ethane subcooler 466 flows to the tube side of the propane subcooler (not shown). The condensed propane exiting the propane surge drum 526 (FIG. 5) flows through the shell side of the propane subcooler. In the propane subcooler, the LP residual gas 464 recovers heat from the condensed propane and raises the temperature by exchange with the condensed propane. The heated LP residual gas 464 is compressed by the fuel gas compressor 472, cooled by the fuel gas compressor aftercooler 474, and then compressed by the sales gas compressor 476.

  The waste heat recovery exchanger 6 cools the LP residual gas 464 after being compressed in the sales gas compressor 476. The heat exchanger 6 recovers waste heat by exchanging with the heating fluid 494. For example, the heat exchanger 6 recovers waste heat between about 100 MMBtu / hour and about 200 MMBtu / hour, such as about 100 MMBtu / hour, about 150 MMBtu / hour, about 200 MMBtu / hour, or another amount of waste heat. it can. The heat exchanger 6 changes the temperature of the heating fluid 494, for example, from the inlet temperature to a temperature between about 260 ° F. and about 280 ° F., for example, about 260 ° F., about 270 ° F., about 280 ° The LP residual gas 464 is cooled while increasing to F or another temperature. The heated heating fluid 494 is sent to a heating fluid system header that carries the heated heating fluid to, for example, a power generation unit or a combined cooling and power generation plant. Compressed and cooled LP residual gas 464 flows to sales gas pipeline 480. The presence of the heat exchanger 6 allows a bypass of the sales gas compressor after the cooler 478, thus saving the total heat duty of the sales gas compressor after the cooler 478.

  Referring to FIG. 5, the propane refrigerant compartment 500 is a three-stage closed loop system that supplies propane refrigerant to the cryogenic trains 402, 404, 406 (FIG. 4). In this propane refrigerant system 500, the compressor 502 compresses the gas from the three propane streams 504, 506, 508 to form a common propane gas header 510. Prior to compression by compressor 502, liquid is removed from propane streams 504, 506, 508 by suction washer 512. Propane streams 504, 506, 508 receive propane vapor from LP economizer 514, high pressure (HP) economizer 515, and propane chillers 206, 440, 448.

  The waste heat recovery exchanger 7 cools the propane gas header 510. The heat exchanger 7 recovers waste heat by exchanging with the heating fluid 594. For example, the heat exchanger 7 has a waste heat between about 700 MMBtu / hour (about 7385539 MJ / h (MW)) and about 800 MMBtu / hour (about 844045 MJ / h (MW)), for example, about 700 MMBtu / hour, 750 MMBtu / hour (about 791292 MJ / h (MW)), about 800 MMBtu / hour, or another amount of waste heat can be recovered. The heat exchanger 7 changes the temperature of the heating fluid 594, for example, from the inlet temperature to a temperature between about 180 ° F. and about 200 ° F., for example about 180 ° F., about 190 ° F., about 200 ° F. The propane gas header 510 is cooled while being raised to ° F, or another temperature. The heated heating fluid 594 is sent to a heating fluid system header that transfers the heated heating fluid to, for example, a power generation unit or a combined cooling and power generation plant.

  In the absence of heat exchanger 7, propane gas header 510 may have a thermal duty between, for example, about 750 MMBtu / hour and about 850 MMBtu / hour (about 896797 MJ / h (MW)), eg, about 750 MMBtu / hour, about 800 MMBtu. Cooled with a propane condenser 522, which can have about 850 MMBtu / hour, or another thermal duty. However, if the propane gas header 510 is cooled by the heat exchanger 7, thereby saving the total heat duty of the propane condenser 522, the propane condenser 522 is not used.

  Following heat exchanger 7, cooled propane gas header 510 flows to one or more propane surge drums 524. The liquid propane 526 exiting the propane surge drum 524 passes through the shell side of a first propane subcooler and a second propane subcooler (collectively illustrated as propane subcooler 528). The first propane subcooler, shown in FIG. 4 as the first supply chiller 412, has an LP residue leaving the ethane subcooler 466 (FIG. 4). The temperature of the liquid propane 526 is lowered by heat exchange with the gas 464. The second propane subcooler further reduces the temperature of the liquid propane 526, for example, by heat exchange with the NGL product from the NGL surge region 470. The second propane subcooler includes a regeneration gas air cooler and a wet regeneration gas chiller (not shown).

  The cooled liquid propane 526 exiting the propane subcooler 528 is flushed to the shell side of the chiller 206 (FIG. 2) in the HP DGA unit and HP economizer 515. The HP economizer 515 stores the propane received from the propane subcooler 528. The top vapor from the HP economizer exits to a third propane gas stream 508 that returns to the suction washer 512. The HP economizer 515 further sends propane to the LP economizer 514, the second feed chiller 440, and a top condenser such as deethanizer. The LP economizer 514 stores the liquid propane from the HP economizer 515. The top vapor from the LP economizer leaves the second propane gas stream 506 that returns to the suction washer 512. The propane liquid in the LP economizer 512 is used in a third propane feed chiller 448 for the ethane condenser downstream of the ethane compressor, which will be discussed below (not shown).

  The liquid recovery unit 400 includes an ethane refrigerant system (not shown), which is a single stage closed loop system that supplies ethane refrigerant to the final supply chiller 456 (FIG. 4). The ethane refrigerant system includes a suction washer that removes ethane liquid from the ethane vapor received from the final supply chiller 456. Ethane vapor flows from the suction cleaner to the ethane compressor. The compressed ethane vapor leaving the ethane compressor passes through the tube side of the ethane condenser, where it is condensed by the propane refrigerant flowing through the shell side of the ethane condenser.

  The condensed ethane flow from the tube side of the ethane condenser accumulates in the ethane surge drum. The condensed ethane from the ethane surge drum uses the LP residual gas 464 on the tube side of the ethane subcooler 466 as a cooling medium, and the shell side of the ethane subcooler 466 (FIG. 4) that lowers the temperature of the condensed ethane. pass. The ethane liquid exiting the ethane subcooler 466 flows into the shell side of the final feed chiller 456 where it is cooled.

  Since the load on the gas processing plant changes seasonally due to demand fluctuations, the load on one or more of the heat exchangers 1 to 7 can change, for example, from season to season. The heat exchangers 1 to 7 can be operated in a partial load operation mode in which the duty of the heat exchangers 1 to 7 is smaller than the full load at which the heat exchanger can operate.

  The heating fluid circuit for flowing the heating fluid through the heat exchangers 1 to 7 can include a plurality of valves that can be operated manually or automatically. For example, a gas processing plant can be equipped with heating fluid flow pipes and valves. The operator can manually open each valve in the circuit to allow heating fluid to flow through the circuit. For example, an operator can manually close each valve in the circuit to perform repairs or maintenance, etc., or to stop waste heat recovery for other reasons. Alternatively, a control system, such as a computer controlled control system, can be connected to each valve in the circuit. The control system can automatically control the valve, for example, based on feedback from sensors (eg, temperature sensors, pressure sensors, or other sensors) installed at various locations in the circuit. An operator can also operate the control system.

  The waste heat recovered from the crude oil associated gas processing plant by the network of heat exchangers 1 to 7 discussed above can be used for power generation, quasi-outside air cooling in the plant, or ambient air conditioning or cooling. Electricity and cold water for cooling can be generated by an energy conversion system, such as an energy conversion system based on an organic Rankine cycle, a carina cycle, or a modified Goswami cycle.

  Referring to FIG. 6, waste heat based on an organic Rankine cycle is converted into electric power using waste heat from a crude oil-associated gas processing plant recovered through a network of heat exchangers 1 to 7 shown in FIGS. Electric power can be supplied to the plant 600 to be operated. The Organic Rankine Cycle (ORC) is an energy conversion system that uses an organic fluid, such as isobutane, in a closed loop configuration. A plant 600 that converts waste heat into electrical power includes a storage tank 602 that stores a heating fluid, such as oil, water, an organic fluid, or another heating fluid. The heating fluid 604 is pumped from the storage tank 602 to the heat exchangers 1 to 7 (FIGS. 1 to 5) by the heating fluid circulation pump 606. For example, the heating fluid 604 can be at a temperature between about 130 ° F and about 150 ° F, such as about 130 ° F, about 140 ° F, about 150 ° F, or another temperature.

  The heated heating fluid from each of the heat exchangers 1 to 7 (eg, the heating fluid heated by waste heat recovery in each of the heat exchangers 1 to 7) merges into a common hot fluid header 608. The hot fluid header 608 can be, for example, a temperature between about 210 ° F and about 230 ° F, such as about 210 ° F, about 220 ° F, about 230 ° F, or another temperature. . The volume of fluid in the hot fluid header 608 is, for example, between about 0.6 MMT / D (million tons / day) and about 0.8 MMT / D, such as about 0.6 MMT / D, about 0.7 MMT / D. D, about 0.8 MMT / D, or another volume.

  Heat from the heated heating fluid heats the ORC working fluid, thereby increasing the pressure and temperature of the working fluid and lowering the temperature of the heating fluid. The heating fluid is then collected in the storage tank 602, pumped through the heat exchangers 1-7 and back to resume the waste heat recovery cycle. The plant 600 that converts waste heat into electric power can generate more power in the winter than in the summer. For example, a plant 600 that converts waste heat into electrical power generates, for example, between about 70 MW and about 90 MW in winter, for example, about 70 MW, about 80 MW, about 90 MW, or another amount of power. In summer, between about 60 and about 80 MW of power can be generated, such as about 60 MW, about 70 MW, about 80 MW, or another amount of power.

  The ORC system 610 includes a pump 612, such as an isobutane pump. The pump 612 may consume, for example, between about 4 MW and about 5 MW of power, for example, about 4 MW, about 4.5 MW, about 5 MW, or another amount of power. The pump 612 supplies isobutane liquid 614, for example, a starting pressure between about 4 bar (0.4 MPa) and about 5 bar (0.5 MPa), for example, about 4 bar, about 4.5 bar (0.45 MPa), about 5 bar. , Or another starting pressure, or higher, eg, an outlet pressure between about 11 bar (1.1 MPa) and about 12 bar, eg, about 11 bar, about 11.5 bar (1.5 MPa), about 12 bar. , Or another outlet pressure. The size of the pump 612 is, for example, between about 0.15 MMT / D and about 0.25 MMT / D isobutane liquid 614, such as about 0.15 MMT / D, about 0.2 MMT / D, about 0.25 MMT. / D, or another amount of isobutane liquid, can be sized to pressurize.

  The isobutane liquid 614 has a thermal duty of, for example, between about 3000 MMBtu / hour (about 3165168 MJ / h (MW)) and about 3500 MMBtu / hour (about 369695 MJ / h (MW)), for example, about 3000 MMBtu / hour, about 3100 MMBtu / hour. (About 3270673 MJ / h (MW)), about 3200 MMBtu / hour (about 3376179 MJ / h (MW)), about 3300 MMBtu / hour (about 3482684 MJ / h (MW)), about 3400 MMBtu / hour (about 3587190 MJ / h (MW)) ), About 3500 MMBtu / hr, or another thermal duty, pumped through an evaporator 616. In the evaporator 616, the isobutane 614 is heated and evaporated by exchange with the hot fluid header 608. For example, the evaporator 616 may remove isobutane 614, for example, at a temperature between about 80 ° F. (about 26.7 ° C.) and about 90 ° F., for example, about 80 ° F., about 85 ° F. 4 ° C), about 90 ° F, or another temperature, for example, between about 150 ° F and about 160 ° F, eg, about 150 ° F, about 155 ° F (about 68.3 ° C). ), Up to about 160 ° F., or another temperature. The pressure of isobutane 614 is reduced, for example, to a pressure between about 10 bar (1.0 MPa) and about 11 bar, such as about 10 bar, about 10.5 bar (1.05 MPa), about 11 bar, or another outlet pressure. . By exchanging with isobutane in the evaporator 616, the hot fluid header 608 can have a temperature of, for example, between about 130 ° F and about 150 ° F, eg, about 130 ° F, about 140 ° F, about 150 ° F, Or cooled to another temperature. The cooled hot fluid header 608 returns to the storage tank 602.

  The heated isobutane 614 provides power to a power turbine 618, such as a gas turbine. The turbine 618 can generate more power in the winter than in the summer in combination with a generator (not shown). For example, the turbine 618 can generate at least about 70 MW in winter, for example, between about 70 MW and about 90 MW, such as about 70 MW, about 80 MW, about 90 MW, or another amount of power. In summer, at least about 60 MW, for example, between about 60 MW and about 80 MW, such as about 60 MW, about 70 MW, about 80 MW, or another amount of power can be generated. Isobutane 614 exits turbine 618 at a lower temperature than the temperature at which it enters turbine 618. For example, isobutane 614 may have a temperature between about 110 ° F. and about 120 ° F. (eg, about 48.9 ° C.), eg, about 110 ° F., about 115 ° F. (about 46.1 ° C.), about 120 ° The turbine 618 may exit at F, or other temperatures.

  The isobutane 614 exiting the turbine 618 is further cooled by replacement with cooling water 622 in a cooler 620, such as an air cooler or cooling water condenser. The cooler 620 may have, for example, a thermal duty between about 2500 MMBtu / hour (about 2637640 MJ / h (MW)) and about 3000 MMBtu / hour, for example, about 2500 MMBtu / hour, about 2600 MMBtu / hour (about 2743145 MJ / h (MW)). , About 2700 MMBtu / hour (about 2848651 MJ / h (MW)), about 2800 MMBtu / hour (about 2954156 MJ / h (MW)), about 2900 MMBtu / hour (about 3059662 MJ / h (MW)), about 3000 MMBtu / hour, or another Thermal duty. The cooler 620 cools the isobutane 614 to various temperatures according to the season of the year, for example, cools the isobutane 614 to a lower temperature in the winter than in the summer. In winter, the cooler 620 can remove isobutane 614 to a temperature between about 60 ° F. (about 15.6 ° C.) and about 80 ° F., for example, about 60 ° F., about 70 ° F. (about 21.1 ° F.). ° C), about 80 ° F, or another temperature. In summer, the cooler 620 brings the isobutane 614 to a temperature between about 80 ° F. and about 100 ° F., eg, about 80 ° F., about 90 ° F., about 100 ° F., or another temperature. Cooling.

  The temperature of the cooling water 622 flowing into the cooler 620 varies depending on the season of the year. For example, in winter, the temperature of the cooling water 622 is between about 55 and about 65 ° F., such as about 55 ° F., about 60 ° F., about 65 ° F., or another temperature. In summer, the temperature of the cooling water 622 is, for example, between about 70 ° F. and about 80 ° F., such as about 70 ° F., about 75 ° F., about 80 ° F., or another temperature. is there. The temperature of the cooling water 622 can be increased by, for example, about 5 ° F., about 10 ° F., about 15 ° F., or another temperature by replacement in the cooler 620. The volume of cooling water 622 flowing through the cooler 620 can be, for example, a volume between about 2.5 MMT / D and about 3.5 MMT / D, such as about 2.5 MMT / D, about 3 MMT / D, about 3 .5MMT / D, or another volume.

  Referring to FIGS. 7A and 7B, cooling with waste heat based on an organic Rankine cycle using waste heat from a crude oil associated gas processing plant recovered through the network of heat exchangers 1 to 7 shown in FIGS. Then, electric power can be supplied to the combined plants 650 and 651 that convert waste heat into electric power. A combined plant 650, 651 that cools with waste heat and converts waste heat into electrical power includes a storage tank 652 that stores a heating fluid, such as oil, water, an organic fluid, or another heating fluid. The heating fluid 654 is pumped from the storage tank 652 to the heat exchangers 1 to 7 (FIGS. 1 to 5) by the heating fluid circulation pump 656. For example, the heating fluid 654 can be at a temperature between about 130 ° F. and about 150 ° F., such as about 130 ° F., about 140 ° F., about 150 ° F., or another temperature. .

  The heated heating fluid from each of the heat exchangers 1-7 (eg, the heating fluid heated by waste heat recovery in each of the heat exchangers 1-7) merges into a common hot fluid header 658. It becomes. The temperature of the hot fluid header 658 can be, for example, a temperature between about 210 ° F. and about 230 ° F., eg, about 210 ° F., about 220 ° F., about 230 ° F., or another temperature. Can do. The volume of fluid in the hot fluid header 658 can be, for example, a volume between about 0.9 MMT / D and about 1.1 MMT / D, such as about 0.9 MMT / D, about 1.0 MMT / D, about 1. 1 MMT / D, or another volume.

  Heat from the heated heating fluid increases the pressure and temperature of the working fluid and lowers the temperature of the heating fluid by heating the ORC working fluid (eg, isobutane). The heating fluid is then collected in the accumulation tank 652, pumped through the heat exchangers 1-7 and back to resume the waste heat recovery cycle. The heated working fluid is used to power the turbine, thus generating power from recovered waste heat from the gas processing plant. In some cases, cooling of the gas stream in the gas treatment plant using the working fluid provides in-plant treatment cooling and enables cooling water cost savings. In some cases, the working fluid is utilized to cool a stream of cooling water used for surrounding air conditioning or cooling in a gas processing plant or nearby industrial community.

  In some cases, a combined system 650 that cools with waste heat and converts waste heat to power can be, for example, between about 40 MW and about 60 MW, such as about 40 MW, about 50 MW, about 60 MW, or another amount of power. , Can be generated. A combined system 650 that cools with waste heat and converts waste heat into electrical power, provides in-plant cooling of the gas stream, cooling of the cooling water to provide mechanical or propane refrigeration, outside air conditioning or cooling, Or both can be replaced. For example, a cooling capacity that replaces a refrigeration load or an air conditioning load between about 60 MW and about 85 MW, such as about 60 MW, about 70 MW, about 80 MW, 85 MW, or another amount of load can be provided.

  Referring specifically to FIG. 7A, the organic Rankine cycle 660 includes a pump 662, such as an isobutane pump. The pump 662 can consume, for example, between about 4 MW and about 5 MW of power, for example, about 4 MW, about 4.5 MW, about 5 MW, or another amount of power. The pump 662 can draw isobutane liquid 664 from, for example, a starting pressure between about 4 bar and about 5 bar, such as about 4 bar, about 4.5 bar, about 5 bar, or another starting pressure, for example higher. , An outlet pressure between about 11 bar and about 12 bar, for example about 11 bar, about 11.5 bar, about 12 bar, or another outlet pressure. The size of the pump 612 is, for example, between about 0.15 MMT / D and about 0.25 MMT / D isobutane liquid 614, such as about 0.15 MMT / D, about 0.2 MMT / D, about 0.25 MMT / D. D, or another amount of isobutane liquid 614, can be sized to be pressurized.

  Isobutane liquid 664 may have a thermal duty of, for example, between 3000 MMBtu / hour and about 3500 MMBtu / hour, for example, about 3000 MMBtu / hour, about 3100 MMBtu / hour, about 3200 MMBtu / hour, about 3300 MMBtu / hour, about 3400 MMBtu / hour, Pumped through an evaporator 666 having 3500 MMBtu / hour, or another thermal duty. In the evaporator 666, the isobutane 664 is heated and evaporated by exchange with the hot fluid header 658. For example, the evaporator 666 can remove isobutane 664 from, for example, a temperature between about 80 ° F. and about 90 ° F., such as about 80 ° F., about 85 ° F., about 90 ° F., or another temperature. For example, to a temperature between about 150 ° F. and about 160 ° F., eg, about 150 ° F., about 155 ° F., about 160 ° F., or another temperature. The pressure of isobutane 664 drops, for example, to between about 10 bar and about 11 bar, such as about 10 bar, about 10.5 bar, about 11 bar, or another outlet pressure. By exchanging with isobutane in the evaporator 666, the hot fluid header 658 has a temperature of, for example, between about 130 ° F and about 150 ° F, eg, about 130 ° F, about 140 ° F, about 150 ° F, Or cooled to another temperature. The cooled hot fluid header 658 returns to the storage tank 652.

  The heated isobutane 664 is divided into two parts, for example, with a split ratio between about 27% and about 38%. In the example of FIG. 7A, the split ratio is 27%. A first portion 676 (eg, about 73%) of heated isobutane 664 provides power to a power turbine 668, eg, a gas turbine. The turbine 668, in combination with a generator (not shown), can generate at least about 50 MW of power, for example between 50 MW and about 70 MW, for example about 50 MW, about 60 MW, about 70 MW, or another amount of power. It is. Isobutane stream 659 exits turbine 668 at a temperature and pressure that is lower than the temperature at which it enters turbine 668. For example, the isobutane stream 659 may have a temperature between about 110 ° F. and about 120 ° F., such as about 110 ° F., about 115 ° F., about 120 ° F., or another temperature, and about 4 bar and about 5 bar. The turbine 668 may exit at a pressure between, for example, about 4 bar, about 4.5 bar, about 5 bar, or another pressure.

  A second portion 678 (eg, about 27%) of heated isobutane 664 flows into ejector 674 as a primary stream. A stream of isobutane vapor 696 from cooling subsystem 685 (discussed in the following paragraph) flows into ejector 674 as a secondary stream. The stream of isobutane 677 joins the isobutane stream 659 that exits the ejector 674 and exits the turbine 668 to form an isobutane stream 680.

  Still referring to FIG. 8, the ejector 674 includes a suction chamber compartment 80 through which heated isobutane 678 and isobutane vapor 696 enter the ejector. The heated isobutane 678 flows through a nozzle 82 having a narrow passage 84 (throat portion) having a minimum cross-sectional area At. Low pressure isobutane vapor 696 flows through low pressure opening 85 having a cross-sectional area of Ae. The two isobutane streams are mixed at a constant pressure in a constant area section 86 having a cross-sectional area of A3. The mixed isobutane exits the ejector through the diffuser compartment 88 as an isobutane stream 677.

  The geometry of the ejector 674 is selected based on the isobutane gas pressure in the isobutane streams 678, 696 entering the ejector and the pressure of the isobutane gas stream 677 exiting the ejector and entering the condenser 670. In the embodiment of FIG. 7 where the split ratio before turbine 668 is between about 27% and about 38% and the split ratio before pump 662 is between about 8% and about 10%, ejector 674 is about It can have an entrainment ratio of 3.5. The ratio (A3: At) of the sectional area A3 of the fixed area section 86 to the sectional area (At) of the passage of the nozzle 84 is 6.4 at the maximum. The ratio (Ae: At) of the cross-sectional area (Ae) of the low-pressure opening 85 to the cross-sectional area (At) of the passage 84 of the nozzle 82 is 2.9 at the maximum.

  The geometric shape of the ejector 674 depends on the gas pressure of isobutane in the system 650. For example, in the embodiment of the cooling and power generation system of FIG. 7 for a gas processing facility, the A3: At ratio is between about 3.3 and about 6.4, for example, about 3.3, about 4, About 4.5, about 5.0, about 5.5, about 6.0, about 6.4, or another ratio. In the particular example of FIG. 7A, the Ae: At ratio is between about 1.3 and about 2.9, such as about 1.3, about 1.5, about 2.0, about 2.5. , About 2.9, or another ratio. The entrainment ratio can be between about 3 and about 5, for example, about 3, about 3.5, about 4, about 4.5, about 5, or another ratio. In some cases, multiple ejectors can be used in parallel. The number of ejectors used in parallel may depend on the isobutane volume flow in streams 678,696.

  Referring again to FIG. 7A, isobutane stream 680 has a temperature between about 110 ° F. and about 120 ° F., eg, about 110 ° F., about 115 ° F., about 120 ° F., or another temperature. be able to. The isobutane stream 680 is further cooled by replacement with cooling water 672 in a cooler 670, such as an air cooler or cooling water condenser. The cooler 670 may have, for example, a thermal duty between about 3000 MMBtu / hour and about 3500 MMBtu / hour, for example, about 3000 MMBtu / hour, about 3100 MMBtu / hour, about 3200 MMBtu / hour, about 3300 MMBtu / hour, about 3400 MMBtu / hour, about Can have 3500 MMBtu / hour, or another thermal duty. The cooler 670 can cool the isobutane 680 to various temperatures depending on the season of the year. For example, the cooler 670 cools the isobutane 680 to a lower temperature in the winter than in the summer. In winter, cooler 670 cools isobutane 680 to a temperature between about 60 ° F. and about 80 ° F., eg, about 60 ° F., about 70 ° F., about 80 ° F., or another temperature. To do. In summer, cooler 670 cools isobutane 680 to a temperature between about 80 ° F. and about 100 ° F., eg, about 80 ° F., about 90 ° F., about 100 ° F., or another temperature. To do.

  The temperature of the cooling water 670 flowing into the cooler 672 varies depending on the season of the year. For example, in winter, the cooling water 672 may have a temperature between about 55 and about 65 ° F., such as about 55 ° F., about 60 ° F., about 65 ° F., or another temperature. it can. In summer, the cooling water 672 has a temperature between, for example, about 70 ° F. and about 80 ° F., eg, about 70 ° F., about 75 ° F., about 80 ° F., or another temperature. be able to. The temperature of the cooling water 672 can be increased by, for example, about 5 ° F., about 10 ° F., about 15 ° F., or another temperature by replacement in the cooler 670. The volume of cooling water 672 flowing through cooler 670 is, for example, a volume between about 2.5 MMT / D and about 3.5 MMT / D, such as about 2.5 MMT / D, about 3 MMT / D, about 3. 5MMT / D, or another volume.

  The cooled isobutane stream 680 is divided into two parts, for example, with a split ratio between about 8% and about 10%. In the illustrated embodiment, the split ratio is about 8%. Isobutane liquid 664 pumped by pump 662 is the first part and includes, for example, a cooled isobutane stream of about 92% volume. A second portion 665 (eg, about 8%) of the cooled isobutane stream 680 is directed to the cooling subsystem 685. The second portion 665 of isobutane passes through a down valve 682 that further cools the isobutane. A down valve 682 cools the isobutane, eg, at a temperature between about 45 ° F. and about 55 ° F., eg, about 45 ° F., about 50 ° F. (about 10 ° C.), about 55 ° F., or Another temperature and, for example, a pressure between about 2 bar (0.2 MPa) and about 3 bar (0.3 MPa), such as about 2 bar, about 2.5 bar (0.25 MPa), about 3 bar, or another Pressure.

  The cooled isobutane released from the down valve 682 is divided into a first portion 684 and a second portion 686, both used for in-plant process cooling. The volume of the first portion 684 and the second portion 686 can be relatively equal. For example, the division ratio of the first portion 684 and the second portion 686 can be about 50%.

  The cooled first portion 684 of isobutane passes through a chiller 688. The chiller 688 has a thermal duty of, for example, between about 50 MMBtu / hour and about 150 MMBtu / hour, for example, about 50 MMBtu / hour, about 60 MMBtu / hour (about 63303 MJ / h (MW)), about 70 MMBtu / hour (about 73854 MJ). / H (MW)), about 80 MMBtu / hour, about 90 MMBtu / hour (about 94955 MJ / h (MW)), about 100 MMBtu / hour, about 110 MMBtu / hour (about 1116056 MJ / h (MW)), about 120 MMBtu / hour, It can have about 130 MMBtu / hour (about 133157 MJ / h (MW)), about 140 MMBtu / hour, about 150 MMBtu / hour, or another thermal duty. Chiller 688 heats isobutane first portion 684 while lowering gas stream 690 in the gas processing plant. In some cases, the gas stream 690 cooled by the chiller 688 can be the feed gas 362 described above. For example, the chiller 688 may move the gas stream 690 from a temperature between about 110 ° F and about 120 ° F, such as about 110 ° F, about 115 ° F, about 120 ° F, or another temperature. The temperature can be reduced to a temperature between about 75 ° F. and about 85 ° F., for example, about 75 ° F., about 80 ° F., about 85 ° F., or another temperature. The chiller 688 moves the isobutane first portion 684 to a temperature between, for example, about 85 ° F. and about 95 ° F. (eg, about 85 ° F., about 90 ° F., about 95 ° F.). F, or another temperature.

  The cooled isobutane second portion 686 passes through a chiller 692. The chiller 692 can have, for example, a thermal duty between about 50 MMBtu / hour and about 150 MMBtu / hour, such as about 50 MMBtu / hour, about 60 MMBtu / hour, about 70 MMBtu / hour, about 80 MMBtu / hour, about 90 MMBtu / hour, about It can have 100 MMBtu / hour, about 110 MMBtu / hour, about 120 MMBtu / hour, about 130 MMBtu / hour, about 140 MMBtu / hour, about 150 MMBtu / hour, or another thermal duty. The chiller 692 may cause the gas stream 694 to enter a gas processing plant at a temperature between about 75 ° F. and about 85 ° F., such as about 75 ° F., about 80 ° F., about 85 ° F., or another The temperature can be reduced to a temperature between about 60 ° F. and about 70 ° F., for example, a temperature of about 60 ° F., about 65 ° F., about 70 ° F., or another temperature. In some cases, the gas stream 694 cooled by the chiller 692 can be the dehydrated feed gas 417 described above. The chiller 692 can remove the second portion 684 of isobutane, for example, at a temperature between about 65 ° F and about 75 ° F, such as about 65 ° F, about 70 ° F, about 75 ° F, or another Can be heated to a temperature.

  By partially cooling the gas stream using the chillers 688 and 692 in the gas processing plant, the cooling load in the gas processing plant is reduced, and thus power saving is possible. For example, if the gas stream 690 cooled by the chiller 688 is the supply gas 362, the cooling load on the components of the first cryogenic train 402 (FIG. 4) can be reduced. Similarly, if the gas stream 694 cooled by the chiller 692 is a dehydrated feed gas 417, the cooling load on the components of the second cryogenic train 404 (FIG. 4) can be reduced.

  The heated first and second portions 684, 686 recombine into an isobutane stream 696 that flows into the ejector 674 as discussed above. The isobutane stream 696 can be, for example, a temperature between about 75 ° F. and about 85 ° F., such as about 75 ° F., about 80 ° F., about 85 ° F., or another temperature, and for example, about 1 A stream of isobutane vapor having a pressure between .5 bar (0.15 MPa) and about 2.5 bar, eg, about 1.5 bar, about 2 bar, about 2.5 bar, or another pressure.

  There are several advantages to using the ejector 674 that contributes to the generation of cooling capacity within the plant. For example, ejectors have lower capital costs than refrigeration components. The use of an ejector reduces the load on such refrigeration components in the gas processing plant, so that smaller and less expensive refrigeration components can be used in the gas processing plant. In addition, the power used to operate the refrigeration components in the gas processing plant can be saved and used elsewhere.

  In some cases, a combined plant 650 that cools with waste heat and converts the waste heat into electrical power can be adjusted to provide different amounts of cooling capacity. For example, the split ratio before the pump 662, the split ratio before the turbine 668, or both can be increased to increase the amount of isobutane supplied to the cooling subsystem 685, thus increasing the amount of cooling at the expense of power generation. The split ratio can be increased as the need for cooling in a gas processing plant increases, for example. For example, the need for cooling gas treatment plants varies from season to season, and the cooling load can be higher in summer than in winter.

  When adjusting the split ratio, the geometry of the ejector 674 can be changed to accommodate changes in the volume of isobutane flowing into the ejector 674. For example, the cross-sectional area (At) of the passage 84 of the nozzle 82, the cross-sectional area (Ae) of the low-pressure opening 85, or the cross-sectional area (A3) of the constant area section 86 can be adjusted. In some cases, a variable ejector can be used to adjust the geometry of the variable ejector based on the split ratio of the system. In some cases, multiple ejectors can be connected in parallel to switch the flow of isobutane streams 678, 696 to an ejector having an appropriate geometry based on the split ratio of the system.

  Referring to FIG. 7B, the organic Rankine cycle 661 can be used for quasi-outside air cooling in a power plant in a gas processing plant, and for example, staff working in the gas processing plant (also referred to as the industrial community of the gas processing plant), nearby non-industrial communities. Or provide ambient air cooling or air conditioning for both.

  The heated isobutane 664 is divided into two parts before the turbine 668, for example with a split ratio between about 27% and about 38%. In the example of FIG. 7B, the split ratio is 38%. As previously described for FIG. 7A, power is generated by a turbine 668 and a generator (not shown). Turbine 668 and the generator may generate at least about 30 MW of power, for example, between about 30 MW and about 50 MW, for example, about 30 MW, about 40 MW, about 50 MW, or another amount of power.

  The cooling capacity is provided by a cooling subsystem 687 that receives a second portion 665 of isobutane from cooler 670. The split ratio of the second and first portions 665, 664 of cooled isobutane 680 can be between about 8% and about 10%, respectively. In the example of FIG. 7B, the split ratio is about 10%. The isobutane second portion 665 cools the isobutane, eg, at a temperature between about 45 ° F and about 55 ° F, eg, about 45 ° F, about 50 ° F, about 55 ° F, or otherwise. And a pressure drop valve 682, for example, between about 2 bar and about 3 bar, eg, about 2 bar, about 2.5 bar, about 3 bar, or another pressure.

  In the cooling subsystem 687, the cooled isobutane released from the down valve 682 is divided into a first portion 673, a second portion 675, and a third portion 671. The isobutane first portion 673 and second portion 675 pass through chillers 688 and 692, respectively, in the gas processing plant, as described above, to cool the gas streams 690 and 694. The cooled third portion 671 of isobutane passes through a chiller 677. The chiller 677 may have, for example, a thermal duty between about 50 MMBtu / hour and about 100 MMBtu / hour, such as about 50 MMBtu / hour, about 60 MMBtu / hour, about 70 MMBtu / hour, about 80 MMBtu / hour, about 90 MMBtu / hour, about It can have 100 MMBtu / hour, or another thermal duty. The chiller 677 can chill a cryogenic water stream 679 that can be used to provide air cooling or air conditioning around an industrial community of a gas processing plant or a nearby non-industrial community. The chiller 677 removes the cold water stream 679 from, for example, a temperature between about 55 ° F. and about 65 ° F., eg, about 55 ° F., about 60 ° F., about 65 ° F., or another temperature. , To a temperature between about 50 ° F. and about 60 ° F., such as about 50 ° F., about 55 ° F., about 60 ° F. or another temperature.

  In the example of FIG. 7B, the first portion 673 receives a 35% volume from isobutane 665 released from the down valve 682, the second portion 675 receives 36% of the volume, and the third portion 671 is 29 Receive%. These volume ratios can be adjusted to adjust the relative amount of industrial cooling capacity and ambient air cooling or air conditioning capacity provided by the cooling subsystem 687. For example, in summer when demand for ambient air cooling or air conditioning increases, the volume of isobutane received by the third portion 671 can increase the ambient air cooling or air conditioning capacity and reduce the industrial cooling capacity. . In some cases, the third portion 671 can receive 100% of the volume of isobutane released from the down valve 682 so that the cooling subsystem 687 provides only ambient air cooling or air conditioning capacity. In some cases, the third portion 671 may allow the cooling subsystem 687 to provide only industrial cooling capacity without receiving flow.

  Upon exiting the cooling subsystem 687, the isobutane first portion 673, second portion 675, and third portion 671 merge into a stream of low pressure isobutane vapor 696 that flows into the ejector 674 as described above. . Stream 696 can be, for example, a temperature between about 70 ° F. and about 80 ° F., such as about 70 ° F., about 75 ° F., about 80 ° F., or another temperature, and It may have a pressure between 5 bar and about 2.5 bar, for example about 1.5 bar, about 2 bar, about 2.5 bar, or another pressure.

  Referring to FIGS. 9A and 9B, waste heat from an associated gas processing plant recovered through a network of heat exchangers 1 to 7 (FIGS. 1-5) is used to convert waste heat from an improved carina cycle to electricity. Electric power can be supplied to the plants 700 and 750 to be converted. The Carina cycle is an energy conversion system that uses a mixture of ammonia and water in a closed loop configuration. In the plant 700 of FIG. 9A, the carina cycle is operated at about 20 bar (2.0 MPa), and in the plant 750 of FIG. 9B, the carina cycle is operated at about 25 bar.

  Each of the plants 700, 750 that convert waste heat into electrical power includes a storage tank 702 that stores a heating fluid, such as oil, water, an organic fluid, or another heating fluid. The heating fluid 704 is pumped from the storage tank 702 to the heat exchangers 1 to 7 (FIGS. 1 to 5) by the heating fluid circulation pump 706. For example, the heating fluid 704 can be at a temperature between about 130 ° F and about 150 ° F, such as about 130 ° F, about 140 ° F, about 150 ° F, or another temperature. .

  The heated heating fluid from each of the heat exchangers 1 to 7 (eg, the heating fluid heated by waste heat recovery in each of the heat exchangers 1 to 7) merges into a common hot fluid header 708. It becomes. The hot fluid header 708 can be, for example, a temperature between about 210 ° F and about 230 ° F, such as about 210 ° F, about 220 ° F, about 230 ° F, or another temperature. . The volume of fluid in the hot fluid header 708 is, for example, between about 0.6 MMT / D and about 0.8 MMT / D, for example, about 0.6 MMT / D, about 0.7 MMT / D, about 0.8 MMT / D. D, or another volume.

  The heat from the hot fluid header 708 is used to heat the ammonia / water mixture in the carina cycle, which is used to power the output turbine and thus generate power from the waste heat recovered from the gas processing plant. In the plant 750, the higher the operating pressure (for example, 25 bar for the plant 750 and 20 bar for the plant 700), the more power generated in the turbine, but the higher the heat exchanger cost. For example, the amount of power generation in the plant 750 is larger than the plant 700 by about 2 MW and about 3 MW, for example, about 2 MW more, about 2.5 MW more, about 3 MW more. Or another larger amount.

  With particular reference to FIG. 9A, a plant 700 for converting waste heat to electricity uses a carina cycle 710 to produce electricity at about 20 bar using an ammonia / water mixture 712 of about 70% ammonia and 30% water. For example, the plant 700 can produce between about 80 MW and about 90 MW of power, such as about 80 MW, about 85 MW, about 90 MW, or another amount of power.

  The carina cycle 710 includes a pump 714. Pump 714 may consume, for example, between about 3.5 MW and about 4.5 MW of power, for example, about 3.5 MW, about 4 MW, about 4.5 MW, or another amount of power. Pump 714 may be used to pump ammonia / water mixture 712, for example, at a starting pressure between about 7 bar (0.7 MPa) and about 8 bar (0.8 MPa), for example, about 7 bar, about 7.5 bar (0.75 MPa), Or an initial pressure of about 8 bar, and higher, eg, an outlet pressure between about 20 bar and about 22 bar, such as about 20 bar, about 21 bar (2.1 MPa), about 22 bar, or another outlet pressure, Can be pressurized. The size of the pump 714 is, for example, between about 0.10 MMT / D and about 0.20 MMT / D, such as about 0.10 MMT / D, about 0.15 MMT / D, about 0.20 MMT / D, or Another amount of ammonia / water mixture 712 can be pressurized.

  The ammonia / water mixture 712 is pumped by a pump 714 to a network of heat exchangers 716, 718, 720, 722 that together use the heat from the heating fluid 704 to achieve partial evaporation of the ammonia / water mixture 712. . The heat exchangers 716 and 720 may have, for example, a thermal duty between about 1000 MMBtu / hour (about 1055060 MJ / h (MW)) and about 1200 MMBtu / hour, eg, about 1000 MMBtu / hour, about 1100 MMBtu / hour (about 1160561 MJ / hour). h (MW)), about 1200 MMBtu / hour, or another thermal duty. The heat exchangers 718 and 722 may have, for example, a thermal duty between about 800 MMBtu / hour and about 1000 MMBtu / hour, for example, about 800 MMBtu / hour, about 900 MMBtu / hour (about 949550 MJ / h (MW)), about 1000 MMBtu / hour. Time, or another thermal duty.

  The ammonia / water mixture 712 leaving the pump 714 can be, for example, a temperature between about 80 ° F. and about 90 ° F., such as about 80 ° F., about 85 ° F., about 90 ° F., or another temperature. , Can have. The ammonia / water mixture 712 from the pump 714 is split into two parts, for example, with a split ratio of about 50%. The first portion 724 of the ammonia / water mixture 712 from the pump 714 is preheated and partially vaporized in the heat exchangers 716 and 718 by exchange with the heating fluid 708. For example, the first portion 724 of the ammonia / water mixture may have a temperature between about 185 ° F. and about 195 ° F. (eg, about 90.6 ° C.), eg, about 185 ° F. (about 85 ° C.), about 190 ° F. Heated to ° F, about 195 ° F, or another temperature. The second portion 732 of the ammonia / water mixture 712 from the pump 714 is preheated in the heat exchanger 720 by exchange with liquid ammonia and water 728 (from the gas-liquid separator 726 described in the following paragraph). It partially vaporizes. For example, the second portion 732 of the ammonia / water mixture may be at a temperature between about 155 ° F and about 165 ° F (about 73.9 ° C), eg, about 155 ° F, about 160 ° F, about 165 ° F. Heated to ° F or another temperature.

  The heated second portion 732 is further heated and partially vaporized in the heat exchanger 722 by exchange with the heating fluid 708. For example, the second portion 732 is further heated to a temperature between about 185 ° F. and about 195 ° F., for example, about 185 ° F., about 190 ° F., about 195 ° F., or another temperature. The

  Heating fluid 708 flowing through the network of heat exchangers 716, 718, 722 cools and returns to storage tank 702. For example, the heating fluid 708 flowing into the network of heat exchangers 716, 718, 722 may have a temperature between about 210 ° F and about 230 ° F, eg, about 210 ° F, about 220 ° F, about 230 ° F. ° F, or another temperature. The heating fluid 708 moves the network of heat exchangers at a temperature between about 130 ° F and about 150 ° F, for example, about 130 ° F, about 140 ° F, about 150 ° F, or another temperature. Get out.

  The heated and partially vaporized first and second portions 724 and 732 flow into a gas-liquid separator 726 that separates liquid ammonia and water from ammonia / water vapor. The pressure in the first and second portions 724 and 732 immediately after entering the separator 724 is, for example, between about 19 bar (1.9 MPa) and about 21 bar, such as about 19 bar, about 20 bar, about 21 bar, or Another pressure. Liquid ammonia and water 728, which are low purity lean streams, exit the bottom of the separator 726, and ammonia / water vapor 730 exits the top of the separator 726.

  A high-purity rich stream ammonia / water vapor 730 generates power (in combination with a generator (not shown)), and in some cases a turbine 734 that can generate different amounts of power in summer and winter. To flow. For example, turbine 734 may provide at least about 60 MW of power during summer, for example, between about 60 MW and about 70 MW, such as about 60 MW, about 65 MW, about 70 MW, or another amount of power during summer. At least about 80 MW of power in winter, for example, between about 80 MW and about 90 MW in winter, for example, about 80 MW, about 85 MW, about 90 MW, or another amount of power, Can be generated. Power is supplied by turbine 734 to a constant volume of ammonia-water vapor 730, for example, a constant volume between about 0.04 MMT / D and about 0.06 MMT / D, for example, 0.04 MMT / D, about Generate with 0.05 MMT / D, about 0.06 MMT / D, or another constant volume. Turbine 734 reduces the pressure of the ammonia / water vapor 730 to a pressure between, for example, about 7 bar and about 8 bar, for example, about 7 bar, about 7.5 bar, about 8 bar, or another pressure. The temperature of the water vapor 730 is, for example, between about 100 ° F. and about 110 ° F., such as about 100 ° F., about 105 ° F. (about 40.6 ° C.), about 110 ° F., or another Reduce to temperature.

  Liquid ammonia and water 728 flow through heat exchanger 720 to a high pressure recovery turbine (HPRT) 736 for further power generation, such as a hydraulic liquid turbine. The HPRT 736 may generate, for example, between about 1 MW and about 2 MW, for example, about 1 MW, about 1.5 MW, about 2 MW, or another amount of power. HPRT 736 provides a constant volume of liquid ammonia and water 728, for example, a constant volume between about 0.05 MMT / D and about 0.15 MMT / D, for example, about 0.05 MMT / D, about 0.1 MMT / D. D, about 0.15 MMT / D, or another constant volume, is used to generate power. The HPRT 736 is capable of adjusting the pressure of liquid ammonia and water 728, for example, between about 7 bar and about 9 bar (0.9 MPa), for example, about 7 bar, about 7.5 bar, about 8 bar, about 8.5 bar (0.85 MPa). , About 9 bar, or another pressure. After exchange in the heat exchanger 720, the liquid ammonia and water 728 may have a temperature between about 100 ° F. and 110 ° F., for example, about 100 ° F., about 105 ° F., about 110 ° F., or Another temperature.

  The ammonia / water vapor 730 and the liquid ammonia and water 728 merge after leaving the turbines 734, 736 to form an ammonia / water mixture 712. The ammonia / water mixture 712 is cooled by replacement with cooling water 740 in a cooler 738, such as a cooling water condenser or air cooler. The cooler 738 may be, for example, a thermal duty between about 2800 MMBtu / hour and about 3200 MMBtu / hour, for example, about 2800 MMBtu / hour, about 2900 MMBtu / hour, about 3000 MMBtu / hour, about 3100 MMBtu / hour, about 3200 MMBtu / hour, or Can have another thermal duty. The cooler 738 cools the ammonia / water mixture 712 to various temperatures according to the season of the year. For example, the cooler 738 cools the ammonia / water mixture 712 to a lower temperature than the summer in winter. In winter, the cooler 738 removes the ammonia-water mixture 712, for example, at a temperature between about 60 ° F. and about 70 ° F., eg, about 60 ° F., about 62 ° F. (about 16.7 ° C.), Cool to about 64 ° F. (about 17.8 ° C.), about 66 ° F. (about 18.9 ° C.), about 68 ° F. (about 20 ° C.), about 70 ° F., or another temperature. In the summer, the cooler 620 can remove isobutane 614 to a temperature between about 80 ° F. and about 90 ° F., eg, about 80 ° F., about 82 ° F. (about 27.8 ° C.), about 84 ° F. (About 28.9 ° C.), about 86 ° F. (about 30 ° C.), about 88 ° F. (about 31.1 ° C.), about 90 ° F., or another temperature.

  The cooling water 740 that flows into the cooler 738 can have various temperatures depending on the season of the year. For example, in winter, the cooling water 740 may have a temperature between about 55 and about 65 ° F., such as about 55 ° F., about 60 ° F., about 65 ° F., or another temperature. it can. In summer, the cooling water 740 has a temperature between about 70 ° F. and about 80 ° F., for example, about 70 ° F., about 75 ° F., about 80 ° F., or another temperature. be able to. The temperature of the cooling water 740 can be increased by, for example, about 15 ° F., about 18 ° F., about 20 ° F., or another temperature by replacement in the cooler 738. The volume of the cooling water 740 flowing through the cooler 738 can be, for example, a volume between about 1.5 MMT / D and about 2.5 MMT / D, such as about 1.5 MMT / D, about 2 MMT / D, about 2. 5MMT / D, or another volume.

  Specifically, referring to FIG. 9B, a plant 750 for converting waste heat to electricity produces electricity at about 25 bar using an ammonia-water mixture 762 of about 78% ammonia and 22% water by a carina cycle 760. To do. For example, plant 750 can produce between about 75 MW and about 95 MW of power, for example, about 75 MW, about 80 MW, about 85 MW, about 90 MW, or another amount of power.

  The carina cycle 760 includes a pump 764. The pump 764 can consume, for example, between about 4.5 MW and about 5.5 MW, for example, about 4.5 MW, about 5 MW, about 5.5 MW, or another amount of power. The pump 764 delivers the ammonia-water mixture 712 at a starting pressure between, for example, about 8.5 bar and about 9.5 bar (0.95 MPa), for example, about 8.5 bar, about 9 bar, or about 9.5 bar. Starting pressure, and higher, eg, outlet pressure between about 24 bar (2.4 MPa) and about 26 bar (2.6 MPa), eg, about 24 bar, about 24.5 bar (2.45 MPa), about It can be pressurized to 25 bar, about 25.5 (2.55 MPa) bar, about 26 bar, or another outlet pressure. The size of the pump 764 can be, for example, an ammonia / water mixture 712 between about 0.10 MMT / D and about 0.20 MMT / D, such as about 0.10 MMT / D, about 0.15 MMT / D, about 0.00. 2MMT / D, or another amount, can be sized to be pressurized.

  Ammonia / water mixture 762 is pumped by pump 764 to network 2 of heat exchangers 766, 768, 770, 77 that together use the heat from heating fluid 704 to achieve partial evaporation of ammonia / water mixture 762. Is done. The heat exchangers 766 and 770 may, for example, have a thermal duty between about 1000 MMBtu / hour and about 1200 MMBtu / hour, such as about 1000 MMBtu / hour, about 1100 MMBtu / hour, about 1200 MMBtu / hour, or another thermal duty. Can have. The heat exchangers 768 and 772 can have, for example, between about 800 MMBtu / hour and about 1000 MMBtu / hour, for example, about 800 MMBtu / hour, about 900 MMBtu / hour, about 1000 MMBtu / hour, or another thermal duty. it can.

  The ammonia / water mixture 762 exiting the pump 764 can be, for example, a temperature between about 80 ° F. and about 90 ° F., such as about 80 ° F., about 85 ° F., about 90 ° F., or another temperature, Have The ammonia / water mixture 762 from the pump 764 is divided into two parts, for example, with a split ratio of about 50%. The first portion 774 (eg, 50%) of the ammonia / water mixture 762 from the pump 764 is preheated and partially vaporized in the heat exchangers 766, 768 by exchange with the heating fluid 704. For example, the first portion 772 of the ammonia / water mixture may be at a temperature between about 170 ° F. (about 76.7 ° C.) and about 180 ° F., eg, about 170 ° F., about 175 ° F. (about 79 ° F.). .4 ° C.), about 180 ° F., or another temperature. A second portion 782 (eg, 50%) of the ammonia / water mixture 762 from the pump 764 is combined with liquid ammonia and water 728 (from the gas-liquid separator 726 described in the following paragraphs) in the heat exchanger 720. Preheated by exchange and partially vaporized. For example, the second portion 782 of the ammonia / water mixture may be at a temperature between about 155 ° F and about 165 ° F, such as about 155 ° F, about 160 ° F, about 165 ° F, or another temperature. , Heated.

  The heated second portion 782 is further heated by the exchange with the heating fluid 708 in the heat exchanger 722 and partially vaporized. For example, the second portion 782 is further heated to a temperature between about 170 ° F. and about 180 ° F., such as about 170 ° F., about 175 ° F., about 180 ° F., or another temperature. The Heating fluid 708 flowing through the network of heat exchangers cools back to storage tank 702. For example, the heating fluid 708 flowing into the network of heat exchangers 716, 718, 722 may have a temperature between about 210 ° F and about 230 ° F, eg, about 210 ° F, about 220 ° F, about 230 ° F. ° F, or another temperature. The heating fluid 708 moves the network of heat exchangers at a temperature between about 130 ° F and about 150 ° F, for example, about 130 ° F, about 140 ° F, about 150 ° F, or another temperature. Get out.

  The heated and partially vaporized first and second portions 774 and 782 flow into a gas-liquid separator 776 that separates liquid ammonia and water from ammonia / water vapor. The pressure in the first and second portions 774 and 782 immediately after entering the separator 776 is, for example, a pressure between about 23 bar (2.3 MPa) and about 25 bar, such as about 23 bar, about 24 bar, about 25 bar, Or another pressure. Liquid ammonia and water 778, which are low purity lean streams, exit the bottom of separator 776, and ammonia / water vapor 780 exits the top of separator 776.

  A high purity pure stream ammonia / water vapor 780 generates power (in combination with a generator (not shown)), and in some cases a turbine 784 that can generate different amounts of power in summer and winter. To flow. For example, turbine 734 may provide between about 65 MW and about 75 MW in summer, for example, about 65 MW, about 70 MW, about 75 MW, or another amount of power, and between about 85 MW and about 95 MW in winter. For example, about 85 MW, about 90 MW, about 95 MW, or another amount of power can be generated. Power is supplied by turbine 784 to a constant volume of ammonia-water vapor 780, for example, a constant volume between about 0.05 MMT / D and about 0.06 MMT / D, for example 0.05 MMT / D, about 0. 0.06 MMT / D, about 0.07 MMT / D, or another volume. The turbine 784 reduces the pressure of the ammonia / water vapor 780 to, for example, a pressure between about 8 bar and about 9 bar, such as about 8 bar, about 8.5 bar, about 9 bar, or another pressure. The temperature of the water vapor 780 is reduced, for example, to a temperature between about 80 ° F. and about 90 ° F., eg, about 80 ° F., about 85 ° F., about 90 ° F., or another temperature.

  Liquid ammonia and water 778 flow via heat exchanger 770 to a high pressure recovery turbine (HPRT) 786, eg, a hydraulic turbine, for further power generation. The HPRT 782 can generate, for example, power between about 1.5 MW and about 2.5 MW, such as about 1.5 MW, about 2 MW, about 2.5 MW, or another amount of power. The power is supplied by HPRT 786 to a constant volume of liquid ammonia and water 778, for example, between about 0.05 MMT / D and about 0.15 MMT / D, for example about 0.05 MMT / D, about 0.1. 1 MMT / D, about 0.15 MMT / D, or another constant volume. HPRT 786 reduces the pressure of liquid ammonia and water 782 to, for example, a pressure between about 8 bar and about 9 bar, such as about 8 bar, about 8.5 bar, about 9 bar, or another pressure. After the exchange in heat exchanger 770, the temperature of liquid ammonia and water 778 can be, for example, a temperature between about 95 ° F and about 105 ° F, eg, about 95 ° F, about 100 ° F, about 105 ° F. F, or another temperature.

  The ammonia / water vapor 780 and the liquid ammonia and water 778 merge after leaving the turbines 784, 786 to form an ammonia / water mixture 762. The ammonia / water mixture 762 is cooled by replacement with cooling water 790 in a cooler 788, such as a cooling water condenser or air cooler. The cooler 788 may have a thermal duty of, for example, between about 2500 MMBtu / hour and about 3000 MMBtu / hour, for example, about 2500 MMBtu / hour, about 2600 MMBtu / hour, about 2700 MMBtu / hour, about 2800 MMBtu / hour, about 2900 MMBtu / hour, about Can have 3000 MMBtu / hour, or another thermal duty. The cooler 788 cools the ammonia / water mixture 762 to various temperatures according to the season of the year. For example, the cooler 788 cools the ammonia / water mixture 762 to a lower temperature in the winter than in the summer. In winter, the cooler 788 removes the ammonia-water mixture 762, for example, at a temperature between about 60 ° F and about 70 ° F, for example, about 60 ° F, about 62 ° F, about 64 ° F, about Cool to 66 ° F, about 68 ° F, about 70 ° F, or another temperature. In summer, the cooler 620 can remove isobutane 614 to temperatures between about 80 ° F. and about 90 ° F., for example, about 80 ° F., about 82 ° F., about 84 ° F., about 86 ° F., about Cool to 88 ° F, about 90 ° F, or another temperature.

  The cooling water 790 flowing into the cooler 788 can have various temperatures depending on the season of the year. For example, in winter, cooling water 790 may have a temperature between about 55 and about 65 ° F., such as about 55 ° F., about 60 ° F., about 65 ° F., or another temperature. it can. In summer, the cooling water 790 has, for example, a temperature between about 70 ° F. and about 80 ° F., such as about 70 ° F., about 75 ° F., about 80 ° F., or another temperature. be able to. The temperature of the cooling water 740 can be increased by, for example, about 15 ° F., about 18 ° F., about 20 ° F., or another temperature by replacement in the cooler 738. The volume of cooling water 740 flowing through cooler 738 can be, for example, a volume between about 1.5 MMT / D and about 2.5 MMT / D, such as about 1.5 MMT / D, about 2 MMT / D, about 2 .5MMT / D, or another volume.

  The carina cycle has its advantages. The carina cycle offers one more degree of freedom than the ORC cycle in that the composition of the ammonia / water mixture can be adjusted. This additional degree of freedom allows the carina cycle to be adapted to specific operating conditions, such as specific heat sources or specific cooling fluids, in order to improve or optimize energy conversion and heat transfer. Furthermore, since ammonia has a molecular weight similar to water, ammonia / water vapors behave similarly to water vapor, so standard steam turbine components can be used. At the same time, the use of a binary fluid allows, for example, changing the composition of the fluid throughout the cycle, providing a richer composition with the evaporator and a leaner composition with the condenser. In addition, ammonia is an environmentally friendly compound and is less dangerous than compounds such as isobutane often used in the ORC cycle.

  Referring to FIGS. 10A and 10B, based on an improved Gosswami cycle utilizing waste heat from a crude oil associated gas processing plant recovered through a network of heat exchangers 716, 718, 722 (FIGS. 1-5). Waste heat can be supplied to the combined cooling and power conversion plants 800, 850. The Goswami cycle is an energy conversion system that uses ammonia and water, eg, a mixture of 50% ammonia and 50% water, in a closed loop configuration. In the embodiment of FIGS. 10A and 10B, each of the improved Goswami cycles 810, 855 are both operated at about 12 bar. The Goswami cycle can generate electricity using low heat source temperatures, such as temperatures below about 200 ° C. The Goswami cycle combines cooling and power generation by combining a Rankine cycle and an absorption refrigeration cycle. In the Goswami cycle turbine, high-concentration ammonia vapor is used. High concentration ammonia can be expanded to very low temperatures without condensing. This very low temperature ammonia can then be used to provide refrigeration output. The improved Goswami cycle 810, 855 enables a large amount of cooling by providing both power generation and cooling functions.

  Each of the combined plants 800, 850 that cool with waste heat and convert waste heat into electrical power each includes a storage tank 802 that stores a heating fluid, such as oil, water, an organic fluid, or another heating fluid. The heating fluid 804 is pumped from the storage tank 802 to the heat exchangers 1 to 7 (FIGS. 1 to 5) by a heating fluid circulation pump 806. For example, the heating fluid 804 can be at a temperature between about 130 ° F. and about 150 ° F., such as about 130 ° F., about 140 ° F., about 150 ° F., or another temperature.

  The heated heating fluid from each of the heat exchangers 1-7 (eg, the heating fluid heated by the recovery of waste heat in each of the heat exchangers 1-7) merges into a common hot fluid header 808. The hot fluid header 808 can be, for example, a temperature between about 210 ° F and about 230 ° F, such as about 210 ° F, about 220 ° F, about 230 ° F, or another temperature. . The volume of fluid in the hot fluid header 808 can be, for example, a volume between about 0.6 MMT / D and about 0.8 MMT / D, for example, about 0.6 MMT / D, about 0.7 MMT / D, about 0.0. 8MMT / D, or another volume.

  Heat from the hot fluid header 808 is utilized to heat the ammonia / water mixture in the modified Goswami cycle 810, 855. Power is supplied to the turbine using a heated ammonia / water mixture. Therefore, electric power is generated from the waste heat recovered from the gas processing plant. The ammonia / water mixture is also used to cool the low temperature water used for semi-outside air cooling in the gas processing plant, thus saving the cost of cooling water. For example, a combined plant 800, 850 that cools with waste heat and converts waste heat into electrical power can be devoted, for example, to about 42% of the base load for quasi-outside air cooling in a gas processing plant.

  Specifically, referring to FIG. 10A, a combined plant 800 that cools with waste heat and converts the waste heat into electrical power is an improved Gosswami that uses an ammonia-water mixture 812 of about 50% ammonia and about 50% water. The cycle 810 can produce electric power and semi-outside air cooling capacity in the cryogenic water plant. For example, the plant 800 can produce between about 50 MW and about 60 MW of power, such as about 50 MW, about 55 MW, about 60 MW, or another amount of power.

  The improved Goswami cycle 810 in the combined plant 800 that cools with waste heat and converts the waste heat into electrical power includes a pump 814. The pump 814 may consume, for example, between about 2.5 MW and about 3.5 MW of power, for example, about 2.5 MW, about 3 MW, about 3.5 MW, or another amount of power. The pump 814 causes the ammonia-water mixture 812 to rise from, for example, an initial pressure between about 3 bar and about 4 bar, such as an initial pressure of about 3 bar, about 3.5 bar, or about 4 bar, for example higher. The outlet pressure can be increased to between about 11.5 bar and about 12.5 bar (1.25 MPa), such as about 11.5 bar, about 12 bar, about 12.5 bar, or another outlet pressure. The size of the pump 814 is, for example, an ammonia / water mixture 812 in an amount between about 0.15 MMT / D and about 0.25 MMT / D, for example, about 0.15 MMT / D, about 0.2 MMT / D, About 0.25 MMT / D, or another amount, can be sized to pressurize the ammonia / water mixture.

  The ammonia / water mixture 812 is pumped by a pump 814 to a network of heat exchangers 816, 818, 820, 822 that together use the heat from the heating fluid 804 to achieve partial evaporation of the ammonia / water mixture 812. The The heat exchangers 816 and 820 are, for example, between about 1300 MMBtu / hour and about 1400 MMBtu / hour (about 1477078 MJ / h (MW)), for example, about 1300 MMBtu / hour, about 1350 MMBtu / hour (about 1424325 MJ / h (MW). )), About 1500 MMBtu / hour, or another thermal duty. The heat exchangers 818 and 822 may have, for example, a heat duty between about 850 MMBtu / hour and about 950 MMBtu / hour (about 1002300 MJ / h (MW)), for example, about 850 MMBtu / hour, about 900 MMBtu / hour, about 950 MMBtu / hour. Time, or another thermal duty.

  The ammonia / water mixture 812 exiting the pump 814 can be, for example, a temperature between about 80 ° F. and about 90 ° F., such as 80 ° F., about 85 ° F., about 90 ° F., or another temperature, Have The ammonia / water mixture 812 is divided into two parts, for example, with a split ratio of about 50%. The first portion 824 (eg, 50%) of the ammonia / water mixture 812 from the pump 814 is preheated and partially vaporized in the heat exchangers 816, 818 by exchange with the heating fluid 808. For example, the first portion 824 of the ammonia / water mixture may be at a temperature between about 190 ° F and about 200 ° F, such as about 190 ° F, about 195 ° F, about 200 ° F, or another temperature. , Heated. A second portion 832 (eg, 50%) of the ammonia / water mixture 812 from the pump 814 is transferred between liquid ammonia and water 828 (from the gas-liquid separator 826 described in the following paragraphs) in the heat exchanger 820. Preheated by exchange and partially vaporized. For example, the second portion 832 of the ammonia / water mixture may be at a temperature between about 165 ° F and about 175 ° F, such as about 165 ° F, about 170 ° F, about 175 ° F, or another temperature. , Heated.

  The heated second portion 832 is further heated in the heat exchanger 822 by, for example, exchange with the heating fluid 804 and partially vaporized. For example, the second portion 832 is further heated to a temperature between about 190 ° F and about 200 ° F, for example, about 190 ° F, about 195 ° F, about 200 ° F, or another temperature. The

  Heating fluid 808 flowing through the network of heat exchangers 816, 818, 822 cools back to the accumulation tank 802. For example, the heating fluid 808 entering the network of heat exchangers 816, 818, 822 may be at a temperature between about 210 ° F and about 230 ° F, eg, about 210 ° F, about 220 ° F, about 230 ° F. ° F, or another temperature. The heating fluid 808 moves the network of heat exchangers at a temperature between about 130 ° F and about 150 ° F, such as about 130 ° F, about 140 ° F, about 150 ° F, or another temperature. Get out.

  The heated and partially vaporized first and second portions 824 and 832 flow into a gas-liquid separator 826 that separates liquid ammonia and water from ammonia / water vapor. The pressure in the first and second portions 824 and 832 immediately after entering the separator 826 is, for example, a pressure between about 10.5 bar and about 11.5 bar, such as about 10.5 bar, about 11 bar, about 11 .5 bar, or another pressure. Liquid ammonia and water 828, which are a low purity lean stream, exit the bottom of the separator 826, and ammonia / water vapor 830, which is a high purity rich stream, exits the top of the separator 826.

  Liquid ammonia and water 828 flow to a high pressure recovery turbine (HPRT) 836, eg, a hydraulic turbine. The HPRT 836 can generate, for example, between about 1 MW and about 2 MW of power, for example, about 1 MW, about 1.5 MW, about 2 MW, or another amount of power. The power is supplied by HPRT 836 to a constant volume of liquid ammonia and water 828, eg, between about 0.15 MMT / D and about 0.2 MMT / D, eg, about 0.15 MMT / D, about 0.1. Generate with 2MMT / D, or another constant volume. HPRT 836 reduces the pressure of liquid ammonia and water 828 to, for example, a pressure between about 3 bar and about 4 bar, eg, about 3 bar, about 3.5 bar (0.35 MPa), about 4 bar, or another pressure. Let After the exchange in heat exchanger 820, the temperature of liquid ammonia and water 828 can be, for example, between about 110 ° F and about 120 ° F, such as about 110 ° F, about 115 ° F, about 120 ° F, Or another temperature.

  The ammonia / water vapor 830 is divided into a first portion 840 and a second portion 842. The split ratio, which is the percentage of steam 830 that is split into the second portion 842, is, for example, between about 10% and about 20%, such as about 10%, about 15%, about 20%, or another split ratio. , And can be. The first portion 840 flows to the turbine 834 and the ammonia / water vapor 830 second portion 842 flows to the water cooler 854 discussed in the following paragraphs. The turbine 834 (in combination with a generator, (not shown)), for example, has a power of at least about 50 MW, eg, between about 50 MW and about 60 MW, eg, about 50 MW, about 55 MW, about 60 MW, or Another amount of power can be generated. The power is supplied by the turbine 834 to a constant volume of ammonia / water vapor 830, eg, between about 0.03 MMT / D and about 0.05 MMT / D, eg, 0.03 MMT / D, about 0. .04MMT / D, about 0.05MMT / D, or another constant volume. The turbine 834 reduces the pressure of the ammonia / water vapor 830 to, for example, a pressure between about 3 bar and about 4 bar, eg, about 3 bar, about 3.5 bar, about 4 bar, or another pressure, The temperature of the water vapor 830 is, for example, a temperature between about 115 ° F and about 125 ° F (about 51.7 ° C), for example, about 115 ° F, about 120 ° F, about 125 ° F, or Lower to another temperature.

  Streams from turbines 834, 836 (first portion of ammonia / water vapor 840 and liquid ammonia and water 828) are cooled by replacement with cooling water 850 in a cooler 846, such as a cooling water condenser or air cooler. To the turbine output stream 848. The cooler 846 may have, for example, a thermal duty between about 2800 MMBtu / hour and about 3200 MMBtu / hour, for example, about 2800 MMBtu / hour, about 2900 MMBtu / hour, about 3000 MMBtu / hour, about 3100 MMBtu / hour, about 3200 MMBtu / hour, or Can have another thermal duty. The cooler 846 cools the turbine output stream 848 to a temperature between about 80 ° F. and about 90 ° F., for example, about 80 ° F., about 85 ° F., about 90 ° F., or another temperature. To do.

  The cooling water 851 entering the cooler 846 can have a temperature between about 70 and about 80 ° F., such as about 70 ° F., about 75 ° F., about 80 ° F., or another temperature. . The cooling water 851 may be replaced by a cooler 846, for example, at a temperature between about 95 ° F and about 110 ° F, such as about 95 ° F, about 100 ° F, about 105 ° F, or another temperature. , Can be heated. The volume of cooling water 851 flowing through the cooler 846 can be, for example, a volume between about 1 MMT / D and about 2 MMT / D, such as about 1 MMT / D, about 1.5 MMT / D, about 2 MMT / D, or another Volume.

  Second portion 842 (also referred to as rich ammonia stream 842) is cooled with a cooler 852, such as a cooling water condenser or an air cooler. The cooler 852 can have, for example, a thermal duty between about 200 MMBtu / hour and about 300 MMBtu / hour, for example, about 200 MMBtu / hour, about 250 MMBtu / hour, about 300 MMBtu / hour, or another thermal duty. . The cooler 852 converts the rich ammonia stream 842 to a temperature between about 80 ° F. and about 90 ° F., for example, about 80 ° F., about 85 ° F., about 90 ° F., or another temperature. Cooling. The cooled rich ammonia stream 842 passes through a down valve 856 that further cools the rich ammonia stream 842. For example, the down valve 856 can stream the rich ammonia stream 842 to a temperature between about 25 ° F. (about −3.89 ° C.) and about 35 ° F. (about 1.67 ° C.), eg, about 25 ° F. Cool to about 30 ° F, about 35 ° F, or another temperature.

  Cooling water 854 entering cooler 852 has a temperature between about 70 ° F. and about 80 ° F., for example, about 70 ° F., about 75 ° F., about 80 ° F., or another temperature. Can do. Cooling water 854 can be replaced by cooler 852, for example, at a temperature between about 80 ° F. and about 90 ° F., eg, about 80 ° F., about 85 ° F., about 90 ° F., or another Temperature. The volume of the cooling water 854 flowing through the cooler 852 is, for example, a volume between about 0.2 MMT / D and about 0.4 MMT / D, such as about 0.2 MMT / D, about 0.3 MMT / D, About 0.4 MMT / D, or another volume.

  The rich ammonia stream 842 discharged from the down valve 856 is used to generate low-temperature water used for semi-outside air cooling in the plant. The first portion 858 of the rich ammonia stream 842 passes through the water chiller 860. The water chiller 860 may have a thermal duty of, for example, between about 50 MMBtu / hour and about 150 MMBtu / hour, for example, about 50 MMBtu / hour, about 60 MMBtu / hour, about 70 MMBtu / hour, about 80 MMBtu / hour, about 90 MMBtu / hour, It may have about 100 MMBtu / hour, about 110 MMBtu / hour, about 120 MMBtu / hour, about 130 MMBtu / hour, about 140 MMBtu / hour, about 150 MMBtu / hour, or another thermal duty. The water chiller 860 heats the cold ammonia stream 862 while heating the first portion 858 of rich ammonia. For example, the water chiller 860 can stream the cold water stream 862 to a temperature between about 95 ° F and about 105 ° F, such as about 95 ° F, about 100 ° F, about 105 ° F, or another temperature. , To a temperature between about 35 ° F. and about 45 ° F., eg, about 35 ° F., about 40 ° F., about 45 ° F., or another temperature. The water chiller 860 can be used to remove the rich ammonia first portion 858, for example, at a temperature between about 85 ° F. and about 95 ° F., eg, about 85 ° F., about 90 ° F., about 95 ° F., or Can be heated to another temperature.

  The second portion 864 of the rich ammonia stream 842 passes through the water chiller 866. The water chiller 866 may have a thermal duty between about 50 MMBtu / hour and about 150 MMBtu / hour, for example, about 50 MMBtu / hour, about 60 MMBtu / hour, about 70 MMBtu / hour, about 80 MMBtu / hour, about 90 MMBtu / hour, It may have about 100 MMBtu / hour, about 110 MMBtu / hour, about 120 MMBtu / hour, about 130 MMBtu / hour, about 140 MMBtu / hour, about 150 MMBtu / hour, or another thermal duty. The water chiller 866 may be used to cool the stream of cold water 868, for example, at a temperature between about 60 ° F and about 70 ° F, such as about 60 ° F, about 65 ° F, about 70 ° F, or another temperature. , To a temperature between about 35 ° F. and about 45 ° F., eg, about 35 ° F., about 40 ° F., about 45 ° F., or another temperature.

  The cryogenic water streams 862, 868 can be used for in-plant cooling in the gas processing plants of FIGS. In some cases, the cryogenic water streams 862, 868 can have a semi-outside air cooling capacity of, for example, between about 200 MMBtu / hr and about 250 MMBtu / hr, for example, about 200 MMBtu / hr, about 210 MMBtu / hr, about 220 MMBtu / hr, A quasi-outside air cooling capacity of about 232112 MJ / h (MW), about 230 MMBtu / hour (about 242663 MJ / h (MW)), about 250 MMBtu / hour, about 250 MMBtu / hour, or another cold water can be produced. In some cases, the rich ammonia stream 842 discharged from the down valve 856 can be used directly for semi-outside air cooling in the plant without using the cold water streams 862, 868 as a buffer.

  Specifically, referring to FIG. 10B, the ammonia-water mixture heated in the combined plant 850 that cools with waste heat and converts the waste heat into electrical power is converted into turbines 834, 836 as described in the previous paragraph. And is used to power an additional turbine 870. The ammonia / water mixture is also used to cool low temperature water used for semi-outside air cooling in the gas processing plant, thus saving cooling water costs. The combined plant 850, which cools with waste heat and converts waste heat into electricity, is powered by an improved Gosswami cycle 855 using an ammonia / water mixture 812 of about 50% ammonia and about 50% water. Quasi-outside air cooling capacity. For example, the plant 850 can produce between about 45 MW and about 55 MW of power, such as about 45 MW, about 50 MW, about 55 MW, or another amount of power. The plant 850 further includes a semi-outside air cooling capacity in the cryogenic water plant between about 200 MMBtu / hr and about 250 MMBtu / hr, such as about 200 MMBtu / hr, about 210 MMBtu / hr, about 220 MMBtu / hr, about 230 MMBtu / hr, about 240 MMBtu / hour (about 253213 MJ / h (MW)), about 250 MMBtu / hour, or another sub-ambient cooling capacity can be produced.

  The ammonia / water vapor 830 is divided into a first portion 872 and a second portion 874. The split ratio, which is the percentage of steam 830 that is split into the second portion 874, is, for example, between about 20% and about 30%, such as about 20%, about 25%, about 30%, or another amount, It can be. First portion 872 flows to turbine 834 and second portion 874 flows to water cooler 876. Turbine 834 (in combination with a generator (not shown)) may use, for example, at least about 40 MW of power, such as about 40 MW, about 42 MW, about 44 MW, about 46 MW, or another, using ammonia / water steam 872. Amount of power, can be generated. Turbine 834 provides a constant volume of ammonia / water vapor 872, for example, a constant volume between about 0.025 MMT / D and about 0.035 MMT / D, such as 0.025 MMT / D, about 0.03 MMT / D. D, about 0.035 MMT / D, or another constant volume, is used to generate power. The turbine 834 reduces the pressure of the ammonia / water vapor 872 to, for example, between about 3 bar and about 4 bar, for example, about 3 bar, about 3.5 bar, about 4 bar, or another pressure, The temperature of the steam 872 is reduced to, for example, between about 115 ° F and about 125 ° F, for example, about 115 ° F, about 120 ° F, about 125 ° F, or another temperature.

  A first portion 872 of ammonia / water vapor from the turbine 834 merges with liquid ammonia and water 828 to form a turbine output stream 848 that is cooled in a cooler 878, such as a cooling water condenser or air cooler. The cooler 878 may have a thermal duty of, for example, between about 2500 MMBtu / hour and about 3000 MMBtu / hour, for example, about 2500 MMBtu / hour, about 2600 MMBtu / hour, about 2700 MMBtu / hour, about 2800 MMBtu / hour, about 2900 MMBtu / hour, about Can have 3000 MMBtu / hour, or another thermal duty. The cooler 878 converts the turbine output stream 848 to, for example, a temperature between about 80 ° F and about 90 ° F, such as about 80 ° F, about 85 ° F, about 90 ° F, or another temperature. Cooling.

  Cooling water 851 flowing into cooler 878 has a temperature between about 70 ° F. and about 80 ° F., for example, about 70 ° F., about 75 ° F., about 80 ° F., or another temperature. Can do. Cooling water 851 may be replaced by cooler 846, for example, at a temperature between about 95 ° F and about 105 ° F, such as about 95 ° F, about 100 ° F, about 105 ° F, or another temperature. , Can be heated. The volume of cooling water 851 flowing through the cooler 846 is, for example, a volume between about 1 MMT / D and about 2 MMT / D, such as about 1 MMT / D, about 1.5 MMT / D, about 2 MMT / D, or Another volume.

  Second portion 874 (also referred to as rich ammonia stream 874) is cooled by cooler 876. The cooler 876 can have, for example, between about 250 MMBtu / hour and about 350 MMBtu / hour, for example, about 250 MMBtu / hour, about 300 MMBtu / hour, about 350 MMBtu / hour, or another thermal duty. The cooler 876 converts the rich ammonia stream 874 to a temperature between about 80 ° F. and about 90 ° F., for example, about 80 ° F., about 85 ° F., about 90 ° F., or another temperature. Cooling. The cooled rich ammonia stream 874 flows into an ammonia / water separator 880 that separates the vapor 882 from the liquid 884 in the rich ammonia stream 874. Steam 882, for example, has a power between about 6 MW and about 7 MW, such as about 6 MW, about 6.5 MW, about 7 MW, or another amount of power (in combination with a generator (not shown)). Flow through the generating turbine 870. Liquid 884 further reduces liquid 884 to a temperature between about 25 and about 35 ° F., for example, about 25 ° F., about 30 ° F., about 35 ° F., or another temperature. Flowing through. Using turbine 870 in addition to turbine 843 helps power conversion plant 850 cope with cooling water temperature fluctuations. For example, the turbine 870 can help compensate for the reduction in power generation that can occur when the temperature of the cooling medium increases (eg, in summer).

  The cooling water 854 entering the cooler 876 can have a temperature between about 70 and about 80 ° F., such as about 70 ° F., about 75 ° F., about 80 ° F., or another temperature. . Cooling water 854 can be replaced with cooler 876, for example, between about 80 ° F. and about 90 ° F., eg, about 80 ° F., about 85 ° F., about 90 ° F., or another temperature. Can be heated. The volume of the cooling water 854 flowing through the cooler 852 is, for example, a volume between about 0.2 MMT / D and about 0.4 MMT / D, such as about 0.2 MMT / D, about 0.3 MMT / D, About 0.4 MMT / D, or another volume.

  Vapor 882 and liquid 884 stream merge to form rich ammonia stream 888. The first portion 890 of the rich ammonia stream 888 passes through the water chiller 860 and the second portion 892 of the rich ammonia stream 888 passes through the water chiller 866. Water chillers 860, 866 operate to provide semi-outside air cooling within the plant, as described in the previous paragraph. In some cases, the rich ammonia stream 888 can be used directly for semi-outside air cooling in the plant without using the cold water streams 862, 868 as a buffer.

  In some cases, the first and second portions 840 and 842 may be combined with parameters of a combined plant 800, 850 that cools with the waste heat described in the previous paragraph and converts the waste heat into electrical power, for example, ammonia / water vapor 830. Operating ratio; ammonia / water concentration in the ammonia / water stream 812; temperature; or other parameters may include, for example, location-specific or environment-specific characteristics, such as ease of cooling water availability Based on changes or constraints on cooling water supply or return temperature. There is a trade-off between the heat exchanger surface area and the amount of power generation or power saving achieved using low temperature water for plant cooling.

  Referring to FIGS. 11A and 11B, the waste heat from the oil-bearing gas processing plant recovered through the network of heat exchangers 1 to 7 (FIGS. 1 to 5) is used to cool with waste heat based on the improved Goswami cycle. Thus, electric power can be supplied to the combined plants 900 and 950 that convert waste heat into electric power. In the example of FIGS. 11A and 11B, the improved Goswami cycle 910, 960 is operated at 12 bar using a mixture of 50% ammonia and 50% water.

  Each of the combined plants 900, 950 that cool with waste heat and convert the waste heat into electrical power includes a storage tank 902 that stores a heating fluid, such as oil, water, an organic fluid, or another heating fluid. The heating fluid 904 is pumped from the accumulation tank 902 to the heat exchangers 1 to 7 (FIGS. 1 to 5) by the heating fluid circulation pump 906. For example, the heating fluid 904 can be at a temperature between about 130 ° F. and about 150 ° F., such as about 130 ° F., about 140 ° F., about 150 ° F., or another temperature. .

  The heated heating fluid from each of the heat exchangers 1 to 7 (eg, the heating fluid heated by waste heat recovery at each of the heat exchangers 1 to 7) merges into a common hot fluid header 908. It becomes. The hot fluid header 908 can be, for example, a temperature between about 210 ° F and about 230 ° F, such as about 210 ° F, about 220 ° F, about 230 ° F, or another temperature. . The volume of fluid in the hot fluid header 908 can be, for example, a volume between about 0.6 MMT / D and about 0.8 MMT / D, such as about 0.6 MMT / D, about 0.7 MMT / D, about 0.0. 8MMT / D, or another volume.

  Heat from the hot fluid header 908 is used to heat the ammonia / water mixture in the modified Goswami cycle 910, 960. The heated ammonia / water mixture is used to power the turbine, thus generating power from the waste heat recovered from the gas processing plant. The ammonia / water mixture is also used for cooling low-temperature water used for semi-outside air cooling in a gas processing plant, thereby saving cooling water costs. In addition, the ammonia / water mixture is used for air conditioning or air cooling for personnel working in the gas treatment plant (also referred to as the gas treatment plant's industrial community), nearby non-industrial communities, or both.

  A combined plant 900, 950 that cools with waste heat and converts waste heat into electrical power is part of a base load for semi-outside air cooling in a gas processing plant, for example, a base between about 40% and about 50%. A portion of the load, such as about 40%, about 42%, about 44%, about 46%, about 48%, about 50%, or a portion of another base load can be covered. Combined plants 900, 950 that cool with waste heat and convert waste heat into electricity can provide outside air cooling for about 2,000 people in the industrial community of gas processing plants. In some cases, a combined plant 900, 950 that cools with waste heat and converts waste heat into electrical power is up to about 40,000 people in a neighboring non-industrial community, for example up to about 35,000 people, up to about 36,000. 000 people, up to about 37,000 people, up to about 38,000 people, up to about 39,000 people, up to about 40,000 people, or another person can provide outside air cooling. In some cases, for example, a combined plant 900 that cools with waste heat and converts the waste heat into electricity to meet an increase or increase in ambient cooling load (eg, on a hot summer day) at the expense of power generation, 950 configurations can be adjusted in real time.

  Specifically, referring to FIG. 11A, an improvement using an ammonia / water mixture 912 of about 50% ammonia and about 50% water in a configuration shown for a combined plant 900 that cools with waste heat and converts the waste heat into electrical power. The type Goswami cycle 910 can produce electric power and low temperature water for cooling the semi-outside air in the plant. For example, the plant 900 can produce between about 45 MW and about 55 MW of power, such as about 45 MW, about 50 MW, about 55 MW, or another amount of power. The plant 900 further includes a semi-outside air cooling capacity in the cryogenic water plant between about 200 MMBtu / hour and about 250 MMBtu / hour, for example, about 200 MMBtu / hour, about 210 MMBtu / hour, about 220 MMBtu / hour, about 230 MMBtu / hour, About 240 MMBtu / hour, about 250 MMBtu / hour, or another sub-ambient cooling capacity can be produced. The combined plant 900, which cools with waste heat and converts waste heat into electricity, is further between about 75 MMBtu / hour (about 79129 MJ / h (MW)) and about 85 MMBtu / hour (about 89680 MJ / h (MW)). Cryogenic water for ambient air conditioning or air cooling can be produced, for example about 75 MMBtu / hour, about 80 MMBtu / hour, about 85 MMBtu / hour, or another amount of ambient water or cold water for air cooling. This amount of cold water can be useful, for example, for up to about 2,000 people working in a gas processing plant. However, by adjusting various parameters of the combined plant 900 that cools with waste heat and converts waste heat into electricity, for example, adding ambient air cooling loads in exchange for lowering the amount of power generated, It is devoted to increasing.

  An improved Goswami cycle 910 in the combined plant 900 that cools with waste heat and converts the waste heat into electrical power includes a pump 914. The pump 914 can consume, for example, between about 2.5 MW and about 3.5 MW, for example, about 2.5 MW, about 3 MW, about 3.5 MW, or another amount of power. The pump 914 causes the ammonia / water mixture 912 to be higher, for example, from an initial pressure between about 3 bar and about 4 bar, such as an initial pressure of about 3 bar, about 3.5 bar, or about 4 bar, for example, , An outlet pressure between about 11 bar and about 13 bar (1.3 MPa), for example about 11 bar, about 12 bar, about 13 bar, or another outlet pressure. The size of the pump 914 is, for example, an ammonia / water mixture 812 in an amount between about 0.15 MMT / D and about 0.25 MMT / D, such as about 0.15 MMT / D, about 0.2 MMT / D, About 0.25 MMT / D, or another amount, can be sized to be pressurized.

  The ammonia / water mixture 912 is pumped by the pump 14 to a network of heat exchangers 916, 918, 920, 922 that together use the heat from the heating fluid 904 to achieve partial evaporation of the ammonia / water mixture 912. The The heat exchangers 916 and 920 may, for example, have a thermal duty between about 1300 MMBtu / hour and about 1400 MMBtu / hour, for example, about 1300 MMBtu / hour, about 1350 MMBtu / hour, about 1500 MMBtu / hour (about 1582584 MJ / h (MW)). ), Or another thermal duty. The heat exchangers 918 and 922 may have, for example, a thermal duty between about 850 MMBtu / hour and about 950 MMBtu / hour, such as about 850 MMBtu / hour, about 900 MMBtu / hour, about 950 MMBtu / hour, or another thermal duty. Can have.

  The ammonia / water mixture 912 exiting the pump 914 can be at a temperature between about 80 ° F. and about 90 ° F., for example, about 80 ° F., about 85 ° F., about 90 ° F., or another temperature. Have. The ammonia / water mixture 912 is divided into two parts, for example, with a split ratio of about 50%. The first portion 924 of the ammonia / water mixture 912 from the pump 914 is preheated and partially vaporized in the heat exchangers 916, 918 by exchange with the heating fluid 908. For example, the first portion 924 of the ammonia / water mixture may be at a temperature between about 190 ° F and about 200 ° F, such as about 190 ° F, about 195 ° F, about 200 ° F, or another temperature. , Heated. The second portion 932 of the ammonia / water mixture 912 from the pump 914 is preheated in the heat exchanger 920 by the exchange of liquid ammonia and water 928 (from the gas-liquid separator 926 described in the following paragraph), It partially vaporizes. For example, the second portion 932 of the ammonia / water mixture may be at a temperature between about 165 ° F. and about 175 ° F., such as about 165 ° F., about 170 ° F., about 175 ° F., or another temperature. , Heated.

  The heated second portion 932 is further heated and partially vaporized in the heat exchanger 922 by exchange with the heating fluid 908. For example, the second portion 932 is further heated to a temperature between about 190 ° F and about 200 ° F, such as about 190 ° F, about 195 ° F, about 200 ° F, or another temperature. The

  Heating fluid 908 flowing through the heat exchanger networks 916, 918, 922 cools back to the accumulation tank 902. For example, the heating fluid 908 entering the heat exchanger networks 916, 918, 922 may be at a temperature between about 210 ° F and about 230 ° F, eg, about 210 ° F, about 220 ° F, about 230 ° F. ° F, or another temperature. The heating fluid 908 moves the network of heat exchangers at a temperature between about 130 ° F and about 150 ° F, for example, about 130 ° F, about 140 ° F, about 150 ° F, or another temperature. Get out.

  The heated and partially vaporized first and second portions 924 and 932 flow into a gas-liquid separator 926 that separates liquid ammonia and water from ammonia / water vapor. The pressure in the first and second portions 924 and 932 immediately after entering the separator 926 is, for example, between about 10.5 bar and about 11.5 bar, such as about 10.5 bar, about 11 bar, about 11. 5 bar, or another pressure. Liquid ammonia and water 928, which are low-purity lean streams, exit the bottom of the separator 926, and ammonia / water vapor 930, which is a high-purity rich stream, exits the top of the separator 926.

  Liquid ammonia and water 928 flow to a high pressure recovery turbine (HPRT) 936, eg, a hydraulic turbine. The HPRT 936 can generate, for example, between about 1 MW and about 2 MW, for example, about 1 MW, about 1.5 MW, about 2 MW, or another amount of power. The power is supplied by HPRT 936 to a constant volume of liquid ammonia and water 928, such as a constant volume between about 0.15 MMT / D and about 0.2 MMT / D, for example about 0.15 MMT / D, about 0. By using 2MMT / D, or another constant volume. HPRT 936 reduces the pressure of liquid ammonia and water 928 to, for example, a pressure between about 3 bar and about 4 bar, such as about 3 bar, about 3.5 bar, about 4 bar, or another pressure. After the exchange in the heat exchanger 920, the temperature of the liquid ammonia and water 928 is, for example, between about 110 ° F and about 120 ° F, such as about 110 ° F, about 115 ° F, about 120 ° F, Or another temperature.

  The ammonia / water vapor 930 is divided into a first portion 940 and a second portion 942. The split ratio, which is the percentage of steam 930 that is split into the second portion 942, is, for example, a split ratio between about 10% and about 20%, such as about 10%, about 15%, about 20%, or Another split ratio can be used. The first portion 940 flows to the turbine 934 and the second portion 942 flows to the cooler 952 discussed in the following paragraph. The first portion 940 is used for power generation. Turbine 934 (in combination with a generator (not shown)) may generate between about 45 MW and about 55 MW of power, for example, about 45 MW, about 50 MW, about 55 MW, or another amount of power. it can. Turbine 934 provides a constant volume of ammonia / water vapor 930, for example, a constant volume between about 0.03 MMT / D and about 0.04 MMT / D, such as 0.03 MMT / D, about 0.035 MMT / D. D, about 0.04 MMT / D, or another constant volume is used to generate power. The turbine 934 reduces the pressure of the ammonia / water vapor 930 to, for example, between about 3 bar and about 4 bar, for example, about 3 bar, about 3.5 bar, about 4 bar, or another pressure, The temperature of 930 is reduced, for example, to a temperature between about 105 ° F. and about 115 ° F., eg, about 105 ° F., about 110 ° F., about 115 ° F., or another temperature.

  Streams from turbines 934, 936 (a first portion of ammonia / water vapor 940 and liquid ammonia and water 928, respectively) are cooled by replacement with cooling water 951 in a cooler 946, eg, a cooling water condenser or air cooler. To the turbine output stream 948. The cooler 946 may have a thermal duty of, for example, between about 2500 MMBtu / hour and about 3000 MMBtu / hour, for example, about 2500 MMBtu / hour, about 2600 MMBtu / hour, about 2700 MMBtu / hour, about 2800 MMBtu / hour, about 2900 MMBtu / hour, about Can have 3000 MMBtu / hour, or another thermal duty. The cooler 946 may move the turbine output stream 948 to a temperature between, for example, about 80 ° F and about 90 ° F, such as about 80 ° F, about 85 ° F, about 90 ° F, or another temperature. Cooling.

  The cooling water 951 entering the cooler 946 can have a temperature between about 70 and about 80 ° F., such as about 70 ° F., about 75 ° F., about 80 ° F., or another temperature. . Cooling water 951 may be replaced by cooler 946, for example, at a temperature between about 95 ° F and about 105 ° F, such as about 95 ° F, about 100 ° F, about 105 ° F, or another temperature. , Can be heated. The volume of cooling water 951 flowing through the cooler 946 is, for example, a volume between about 1 MMT / D and about 2 MMT / D, such as about 1 MMT / D, about 1.5 MMT / D, about 2 MMT / D, or Another volume.

  The second portion 942 (also referred to as rich ammonia stream 942) is used for cooling. The rich ammonia stream 942 is cooled in a cooler 952, such as a cooling water condenser or an air cooler. The cooler 952 can have, for example, a thermal duty between about 300 MMBtu / hour and about 400 MMBtu / hour, eg, about 300 MMBtu / hour, about 350 MMBtu / hour, about 400 MMBtu / hour, or another thermal duty. The cooler 952 converts the rich ammonia stream 942 to a temperature between about 80 ° F. and about 90 ° F., for example, about 80 ° F., about 85 ° F., about 90 ° F., or another temperature. Cooling. The cooled rich ammonia stream 942 passes through a down valve 956 that further cools the rich ammonia stream 942. For example, the down valve 956 can bring the rich ammonia stream 942 to a temperature between about 25 ° F. and about 35 ° F., eg, about 25 ° F., about 30 ° F., about 35 ° F., or another temperature. Cooling.

  Cooling water 954 flowing into cooler 952 has a temperature between about 70 ° F. and about 80 ° F., for example, about 70 ° F., about 75 ° F., about 80 ° F., or another temperature. Can do. Cooling water 954 can be replaced by cooler 952, for example, at a temperature between about 80 ° F. and about 90 ° F., eg, about 80 ° F., about 85 ° F., about 90 ° F., or another temperature. , Can be heated. The volume of cooling water 954 flowing through the cooler 952 is, for example, a volume between about 0.3 MMT / D and about 0.5 MMT / D, for example, about 0.3 MMT / D, about 0.4 MMT / D, It can be about 0.5 MMT / D, or another volume.

  The rich ammonia stream 942 discharged from the down valve 956 is used to generate semi-outside air cooling in the plant and low-temperature water used for air conditioning or air cooling in the plant. The first portion 958 and the second portion 964 of the rich ammonia stream 942 are used for semi-outside air cooling in the plant. A first portion 958 of the rich ammonia stream 942 passes through a water chiller 960. The water chiller 960 can have a thermal duty of, for example, between about 50 MMBtu / hour and about 150 MMBtu / hour, such as about 50 MMBtu / hour, about 60 MMBtu / hour, about 70 MMBtu / hour, about 80 MMBtu / hour, about 90 MMBtu / hour, It may have about 100 MMBtu / hour, about 110 MMBtu / hour, about 120 MMBtu / hour, about 130 MMBtu / hour, about 140 MMBtu / hour, about 150 MMBtu / hour, or another thermal duty. The water chiller 960 can heat the cold water stream 962 while heating the first portion 958 of rich ammonia. For example, the water chiller 960 may cause the stream of cold water 962 to be at a temperature between about 95 ° F and about 105 ° F, such as about 95 ° F, about 100 ° F, about 105 ° F, or another temperature. , To a temperature between about 35 ° F. and about 45 ° F., eg, about 35 ° F., about 40 ° F., about 45 ° F., or another temperature. The water chiller 960 may remove the first portion 958 of rich ammonia, for example, at a temperature between about 85 ° F and about 95 ° F, such as about 85 ° F, about 90 ° F, about 95 ° F, or Can be heated to another temperature.

  A second portion 964 of the rich ammonia stream 942 passes through the water chiller 966. The water chiller 866 may have a thermal duty between about 50 MMBtu / hour and about 150 MMBtu / hour, for example, about 50 MMBtu / hour, about 60 MMBtu / hour, about 70 MMBtu / hour, about 80 MMBtu / hour, about 90 MMBtu / hour, It may have about 100 MMBtu / hour, about 110 MMBtu / hour, about 120 MMBtu / hour, about 130 MMBtu / hour, about 140 MMBtu / hour, about 150 MMBtu / hour, or another thermal duty. The water chiller 966 may cause the stream of cold water 968 to flow at a temperature between about 60 ° F. and about 70 ° F., such as about 60 ° F., about 65 ° F., about 70 ° F., or another temperature, for example. , To a temperature between about 35 ° F. and about 45 ° F., eg, about 35 ° F., about 40 ° F., about 45 ° F., or another temperature.

  The cryogenic water streams 962, 968 can be used for in-plant cooling in the gas processing plants of FIGS. In some cases, the cryogenic water streams 962, 968 may have a cold level outdoor air cooling capacity of, for example, between about 200 MMBtu / hour and about 250 MMBtu / hour, such as about 200 MMBtu / hour, about 210 MMBtu / hour, about 220 MMBtu / hour, About 230 MMBtu / hour, about 250 MMBtu / hour, about 250 MMBtu / hour, or another amount of cold level outdoor air cooling capacity can be produced. In some cases, the rich ammonia stream 942 released from the down valve 956 can be used directly for semi-outside air cooling in the plant without using the cryogenic water streams 962, 968 as a buffer.

  A third portion 970 of the rich ammonia stream 942 is used for air conditioning or air cooling in the plant. A third portion 970 of the rich ammonia stream 942 passes through the water chiller 972. The water chiller 972 may have, for example, a thermal duty between about 75 MMBtu / hour and about 85 MMBtu / hour, such as about 85 MMBtu / hour, about 80 MMBtu / hour, about 85 MMBtu / hour, or another thermal duty. it can. The water chiller can heat the cold water stream 974 while heating the first portion 970 of rich ammonia. For example, the water chiller 972 may cause the stream of cold water 974 to be at a temperature between about 40 ° F. and about 50 ° F., such as about 40 ° F., about 45 ° F., about 50 ° F., or another temperature. , To a temperature between about 35 ° F. and about 45 ° F., eg, about 35 ° F., about 40 ° F., about 45 ° F., or another temperature. The water chiller 972 moves the rich ammonia third portion 970 to a temperature between about 30 ° F. and about 40 ° F., for example, about 30 ° F., about 35 ° F., about 40 ° F., or Can be heated to another temperature. The cryogenic water stream 974 is used for air cooling or air conditioning in the industrial community of a gas processing plant. The cryogenic water stream 974 can be, for example, between about 75 MMBtu / hour and about 85 MMBtu / hour of air-cooled or air-conditioned cryogenic water, such as about 75 MMBtu / hour, about 80 MMBtu / hour, about 85 MMBtu / hour, or another amount. Low temperature water.

  In some cases, for example, the split ratio between the first portion 940 and the second portion of the ammonia / water vapor 930 can be changed to meet additional or greater cooling loads. For example, the split ratio can be, for example, 10%, 15%, 20%, 30%, 40%, 50%, or another ratio. For example, the division ratio can be increased in summer so as to satisfy the additional air cooling requirement due to a rise in ambient temperature, while the division ratio can be increased in winter when the surrounding cooling is not so much used.

  Referring to FIG. 11B, the cooling power conversion combined plant 950 can be configured only for cooling with little or no power generation. The cooling power conversion combined plant 950 performs substantially the same operation as that of the cooling power conversion combined plant 900. However, all ammonia / water vapor 930 is directed to the rich ammonia stream 942 for cooling purposes, and no ammonia / water vapor is sent to the turbine 934. That is, the division ratio is 100%.

  In the illustrated configuration, a combined plant 950 that cools with waste heat and converts the waste heat into electrical power is generated by an improved Goswami cycle 960 that uses an ammonia / water mixture 912 of about 50% ammonia and about 50% water. Can produce low temperature water for cooling of semi-outside air and low temperature water for ambient air conditioning or air cooling. For example, the plant 950 has a semi-outside air cooling capacity in a cryogenic water plant between about 200 MMBtu / hour and about 250 MMBtu / hour, for example, about 200 MMBtu / hour, about 210 MMBtu / hour, about 220 MMBtu / hour, about 230 MMBtu / hour. , About 240 MMBtu / hr (about 253213 MJ / h (MW)), about 250 MMBtu / hr, or another sub-ambient cooling capacity. The plant 950 further includes ambient water or air cooled cryogenic water between about 1200 MMBtu / hour and about 1400 MMBtu / hour, for example, about 1200 MMBtu / hour, about 1300 MMBtu / hour, about 1400 MMBtu / hour, or another amount of ambient Low temperature water for air conditioning or cooling capacity can be produced. This amount of cold water can provide, for example, a cooling capacity of up to about 2,000 people in the industrial community of a gas treatment plant and about 31,000 people in a neighboring non-industrial community.

  The rich ammonia stream 942 is cooled in a cooler 953, such as a cooling water condenser or an air cooler. The cooler 953 may have a thermal duty between about 2000 MMBtu / hour (about 2110112 MJ / h (MW)) and about 2500 MMBtu / hour, for example, about 2000 MMBtu / hour, about 2100 MMBtu / hour (about 2215617 MJ / h (MW)). ), About 2200 MMBtu / hour (about 2321123 MJ / h (MW)), about 2300 MMBtu / hour (about 2426628 MJ / h (MW)), about 2400 MMBtu / hour (about 2532134 MJ / h (MW)), about 2500 MMBtu / hour, or Can have another thermal duty. The cooler 953 converts the rich ammonia stream 942 to a temperature between about 80 ° F. and about 90 ° F., for example, about 80 ° F., about 85 ° F., about 90 ° F., or another temperature. Cooling. The cooled rich ammonia stream 942 passes through a down valve 956 that further cools the rich ammonia stream 942. For example, the down valve 956 may cause the rich ammonia stream 942 to flow at a temperature between about 25 ° F. and about 35 ° F., such as about 25 ° F., about 30 ° F., about 35 ° F., or another temperature, Can be cooled.

  The cooling water 954 entering the cooler 952 can have a temperature between about 70 and about 80 ° F., such as about 70 ° F., about 75 ° F., about 80 ° F., or another temperature. . Cooling water 954 may be replaced by cooler 953, for example, at a temperature between about 80 ° F. and about 90 ° F., such as about 80 ° F., about 85 ° F., about 90 ° F., or another temperature, Can be heated. The volume of cooling water 954 flowing through the cooler 953 is, for example, a volume between about 2 MMT / D and about 3 MMT / D, such as about 2 MMT / D, about 2.5 MMT / D, about 3 MMT / D, or Another volume.

  The rich ammonia stream 942 discharged from the down valve 956 is used to generate semi-outside air cooling in the plant and low temperature water used for air conditioning or air cooling in the plant. As described in the previous paragraph, the first portion 958 and the second portion 964 of the rich ammonia stream 942 are exchanged with the cryogenic water streams 962, 968 in the water chillers 960, 966, for example, by sub-outside air in the plant. Used for cooling. In some cases, the cryogenic water streams 962, 968 may have a cold level outdoor air cooling capacity of, for example, between about 200 MMBtu / hour and about 250 MMBtu / hour, such as about 200 MMBtu / hour, about 210 MMBtu / hour, about 220 MMBtu / hour, About 230 MMBtu / hour, about 250 MMBtu / hour, about 250 MMBtu / hour, or another amount of cold level outdoor air cooling capacity can be produced. In some cases, the rich ammonia stream 942 released from the down valve 956 can be used directly for semi-outside air cooling in the plant without using the cryogenic water streams 962, 968 as a buffer.

  The third portion 970 of the rich ammonia stream 942 is used for in-plant air conditioning or air cooling. A third portion 970 of the rich ammonia stream 942 passes through the water chiller 973. The water chiller 973 can have, for example, a thermal duty between about 1200 MMBtu / hour and about 1400 MMBtu / hour, such as about 1200 MMBtu / hour, about 1300 MMBtu / hour, about 1400 MMBtu / hour, or another thermal duty. it can. The water chiller 973 can heat the cold ammonia stream 974 while heating the third portion 970 of rich ammonia. For example, the water chiller 973 may cause the stream of cold water 974 to be at a temperature between about 40 ° F. and about 50 ° F., such as about 40 ° F., about 45 ° F., about 50 ° F., or another temperature. , To a temperature between about 35 ° F. and about 45 ° F., eg, about 35 ° F., about 40 ° F., about 45 ° F., or another temperature. The water chiller 973 can be used to remove the third portion 970 of rich ammonia, for example, at a temperature between about 30 ° F. and about 40 ° F., eg, about 30 ° F., about 35 ° F., about 40 ° F., or Can be heated to another temperature. The cryogenic water stream 974 is used for air cooling or air conditioning in the industrial community of a gas processing plant. The cryogenic water stream 974 can be, for example, between about 1200 MMBtu / hour and about 1400 MMBtu / hour of air-cooled or air-conditioned cryogenic water, such as about 1200 MMBtu / hour, about 1300 MMBtu / hour, about 1400 MMBtu / hour, or another amount. Air cooling or low temperature water for air conditioning. This amount of cryogenic water can provide, for example, a cooling capacity of about 2,000 employees working in the industrial community of a gas processing plant and about 31,000 employees working in an adjacent non-industrial community.

  Referring to FIG. 12, the waste heat from the crude oil gas treatment plant recovered through the network of heat exchangers 1 to 7 (FIGS. 1-5) is configured solely for cooling with little or no power generation. It can be used to supply power to a combined plant 980 that cools with waste heat based on the improved Gossami cycle and converts the waste heat to electricity. The cooling and power conversion combined plant 980 performs substantially the same operation as that of the cooling and power conversion combined plant 900 and 950 described above. The configuration of the plant 980 can provide quasi-outside air cooling and air conditioning or air cooling cryogenic water in the plant by an improved Gosswa cycle 990 using an ammonia / water mixture 912 of about 50% ammonia and about 50% water. For example, the plant 980 may have a semi-outside air cooling capacity in a cryogenic water plant between about 200 MMBtu / hour and about 250 MMBtu / hour, eg, about 200 MMBtu / hour, about 210 MMBtu / hour, about 220 MMBtu / hour, about 230 MMBtu / hour. About 240 MMBtu / hour, about 250 MMBtu / hour, or another amount of semi-outside air cooling capacity in the cryogenic water plant. Plant 980 further includes ambient air or cold water for air cooling between about 1400 MMBtu / hour and about 1600 MMBtu / hour (about 1688089 MJ / h (MW)), eg, about 1400 MMBtu / hour, about 1500 MMBtu / hour, about 1600 MMBtu. Per hour, or another amount of ambient air conditioning or cold water for cooling capacity. This amount of cold water can provide, for example, a cooling capacity of about 2,000 people in the industrial community of a gas processing plant and about 35,000 people in a neighboring non-industrial community.

  In the plant 980, a rectifying column 982, for example, a 4-tray (shelf) rectifying column is used in place of the separator 926 (FIGS. 11A and 11B). The rectification column 982 receives an ammonia / water mixture feed 984. The feed 984 can have, for example, a temperature between about 80 ° F. and about 90 ° F., such as about 80 ° F., about 85 ° F., about 90 ° F., or another temperature, The pressure may be between about 10 bar and about 15 bar (1.5 MPa), for example, about 10 bar, about 11 bar, about 12 bar, about 13 bar, about 14 bar, about 15 bar, or another pressure. The split ratio of feed 984 to rectification column 982 can be, for example, up to about 5% of ammonia / water mixture 912, such as about 1%, about 2%, about 3%, about 4%, about%, or another Division ratio. The remaining ammonia / water mixture 912 is evenly divided into first and second portions 924 and 932. The split ratio of the first and second portions 924 and 932 and the supply 994 determines the cooling load and can provide, for example, up to about 13% flexibility in changing cooling demand.

  The overhead discharge 986 from the rectification column 982, containing high purity ammonia, flows to the water cooler 955, from which the overhead discharge 986 provides cooling capacity to the chillers 960, 966 and the water chiller 975. The water chiller 975 has a thermal duty between about 1200 MMBtu / hour and about 1600 MMBtu / hour, for example about 1200 MMBtu / hour, about 1300 MMBtu / hour, about 1400 MMBtu / hour, about 1500 MMBtu / hour, about 1600 MMBtu / hour, or another Thermal duty. The water chiller 975 can heat the cryogenic water stream 974 while heating the third portion 970 of rich ammonia. For example, the water chiller 975 may cause the stream of cold water 974 to have a temperature between about 40 ° F and about 50 ° F, such as about 40 ° F, about 45 ° F, about 50 ° F, or another temperature. , To a temperature between about 35 ° F. and about 45 ° F., eg, about 35 ° F., about 40 ° F., about 45 ° F., or another temperature. The water chiller 975 can remove the third portion 970 of rich ammonia, for example, at a temperature between about 30 ° F and about 40 ° F, such as about 30 ° F, about 35 ° F, about 40 ° F, or otherwise. Can be heated to The bottom stream 990 from the rectification column 982 flows to the turbine 936 via the heat exchanger 920.

  In some cases, the parameters of the combined plants 900, 950, 980 that cool with the waste heat described in the previous paragraph and convert the waste heat into electric power, for example, ammonia and water vapor 930, are provided in the first and second portions 940 and Operating pressure; ammonia / water concentration in the ammonia / water stream 912; or other parameters, for example, location-specific or environment-specific characteristics, such as changes in the availability of cooling water Or a restriction on the supply or return temperature of the cooling water. There is a trade-off between the heat exchanger surface area and the amount of power generation or power saving achieved using low temperature water for plant cooling.

  Excess cooling capacity may be generated in a combined plant that cools with the waste heat and converts the waste heat into electrical power. Excess cooling capacity can be sent to a cooling grid used for other applications.

  Other implementations are within the scope of the following claims.

1-7 Heat exchangers 104, 106 Slag catcher 146 Condensate pump 166 Stripper tower 176 Sour water recirculation pump 200 High pressure gas processing section 202 Gas processing area 204 Dehydration unit 222, 322 DGA stripper 234, 334 DGA circulation pump 268 TEG stripper 282 Lean TEG circulation pump 300 Low pressure gas processing section 302 Gas processing region 304 Supply gas compression region 346 Stripper recirculation pump 400 Liquid recovery unit 402 First low temperature train 404 Second low temperature train 406 Third low temperature train 408 Demethanizer Division 424 Liquid dehydrator supply pump 441 Demethanizer tower reboiler pump 462 Demethanizer tower bottom pump 500 Propane refrigerant compartment 600, 700, 750 Plant 602, 652, 70 , 802, 902 Accumulation tank 606, 656, 706, 806, 906 Heating fluid circulation pump 610 ORC system 612, 662 Pump 616, 666 Evaporator 618 Turbine 650, 651 Combined plant 660, 661 Organic Rankine cycle 674 Ejector 710, 760 Carina cycle 714, 764, 814, 914 Pump 800, 850, 900, 950, 980 Power conversion combined plant 810, 855, 910, 960 Improved Goswami cycle

Claims (29)

A waste heat recovery heat exchanger configured to heat the heating fluid stream by exchange with a heat source in a crude oil associated gas processing plant;
An organic Rankine cycle energy conversion system;
The organic Rankine cycle energy conversion system is:
An energy conversion heat exchanger configured to heat a first portion of the working fluid comprising isobutane by exchange with the heated heating fluid stream;
One or more configured to cool one or more of a process stream from the crude oil associated gas processing plant and a cooling water stream for cooling the outside air by replacement with a second portion of the working fluid; A cooling subsystem including a plurality of cooling elements;
Receiving the second portion of the working fluid from the cooling subsystem and a third portion of the working fluid that is part of the heated first portion of the working fluid. An ejector to do;
A turbine and a generator configured to generate power by expansion of a fourth portion of the working fluid that is part of the heated first portion of the working fluid;
A cooling element configured to cool a stream of working fluid that includes an output stream of working fluid from the ejector and the expanded fourth portion of the working fluid from the turbine and generator. And having
system. The stream of working fluid output from the cooling element is divided into the first portion of the working fluid and the second portion of the working fluid;
The system of claim 1. The ejector geometry is: (i) the ratio of the amount of working fluid in the first portion of the working fluid to the amount of working fluid in the second portion of the working fluid; and (Ii) based on one or more of the ratio of the amount of working fluid in the third portion of the working fluid to the amount of working fluid in the fourth portion of the working fluid; It is determined,
The system of claim 1. The ratio of the amount of working fluid in the first portion of the working fluid to the amount of working fluid in the second portion of the working fluid is between about 0.90 and about 0.92. And the ratio of the amount of working fluid in the third portion of the working fluid to the amount of working fluid in the fourth portion of the working fluid is about 0.27 and about 0.38. Between
The system of claim 1. The ejector entrainment ratio is 3.5,
The system according to claim 4. The ratio of the cross-sectional area of the fixed area section of the ejector to the cross-sectional area of the throat section of the ejector nozzle is about 6.4;
The ratio of the cross-sectional area of the low-pressure opening of the ejector to the cross-sectional area of the throat portion of the nozzle of the ejector is about 2.9.
The system according to claim 4. The temperature of the second portion of the working fluid is between 45 ° F. and 55 ° F. upon entering the cooling subsystem and 75 ° F. and 85 ° F. upon exiting the cooling subsystem. Between
The system of claim 1. The cooling subsystem includes
At least one first cooling element configured to cool the process stream from the crude oil associated gas processing plant;
At least one second cooling element configured to cool the cooling water stream for outside air cooling;
The system of claim 1. The ratio of the volume of working fluid flowing through the at least one first cooling element to the volume of working fluid flowing through the at least one second cooling element is adjustable.
The system according to claim 8. The energy conversion heat exchanger is configured to heat the first portion of the working fluid to a temperature between 150 ° F. and 160 ° F.
The system of claim 1. Comprising a plurality of ejectors connected in parallel;
The system of claim 1. The cooling subsystem is configured to produce a cooling capacity between 60 MW and 85 MW;
The system of claim 1. The turbine and generator are configured to generate power between 30 MW and 60 MW,
The system of claim 1. Comprising a pump configured to boost the first portion of the working fluid to a pressure between 11 bar and 12 bar;
The system of claim 1. The cooling element is configured to cool the working fluid from a temperature between 110 ° F. and 120 ° F. to a temperature between 80 ° F. and 90 ° F.
The system of claim 1. Comprising a storage tank, the heating fluid flows from the storage tank through the waste heat recovery heat exchanger, through the organic Rankine cycle energy conversion system, and back to the storage tank;
The system of claim 1. The waste heat recovery heat exchanger is configured to heat the heating fluid stream by exchange with a steam stream from a slag catcher in an inlet region of the gas processing plant;
The system of claim 1. The waste heat recovery heat exchanger is configured to heat the heating fluid stream by exchange with an output stream from a DGA stripper in the gas processing plant.
The system of claim 1. The waste heat recovery heat exchanger is configured to heat the heating fluid stream by exchange with one or more of a sweet gas stream and a sales gas stream in the gas processing plant.
The system of claim 1. The waste heat recovery heat exchanger is configured to heat the heating fluid stream by replacement with a propane header in a propane refrigeration unit of the gas processing plant in the gas processing plant.
The system of claim 1. Heating the heating fluid stream via a waste heat recovery heat exchanger by exchanging with a heat source in a crude oil associated gas processing plant;
Generating power and cooling capacity in an organic Rankine cycle energy conversion system;
Generating the power and cooling capacity comprises:
Heating a first portion of the working fluid comprising isobutane by exchange with the heated heating fluid stream via an energy conversion heat exchanger;
Cooling one or more of a process stream from the crude oil associated gas processing plant and a cooling water stream for cooling outside air by exchanging with a second portion of the working fluid in a cooling subsystem;
In an ejector, the second portion of the working fluid from the cooling subsystem and a third portion of the working fluid that is part of the heated first portion of the working fluid; Mixing, and;
Generating power by expansion of a fourth portion of the working fluid that is part of the heated first portion of the working fluid in a turbine and a generator;
Cooling a working fluid stream comprising an output stream of working fluid from the ejector and the expanded fourth portion of the working fluid from the turbine and generator;
Method. Dividing the stream of working fluid output from the cooling element into the first portion of the working fluid and the second portion of the working fluid;
The method of claim 21. (I) a ratio of the amount of working fluid in the first portion of the working fluid to the amount of working fluid in the second portion of the working fluid; and (ii) the amount of working fluid in the first portion. Adjusting one or more of the ratio of the amount of working fluid in the third portion and the amount of working fluid in the fourth portion of the working fluid;
The method of claim 21. Adjusting one or more of the ratios based on a target cooling capacity,
24. The method of claim 23. Connecting the ejector to the organic Rankine cycle energy conversion system, wherein the ejector is selected based on one or more of the ratios;
24. The method of claim 23. Cooling one or more of the process stream and the cooling water stream in a cooling subsystem comprises producing a cooling capacity between 60 MW and 85 MW.
The method of claim 21. Generating power comprises generating power between 40 MW and 60 MW,
The method of claim 21. Boosting the first portion of the working fluid to a pressure between 11 bar and 12 bar;
The method of claim 21. Flowing the heating fluid stream from an accumulation tank through the waste heat recovery heat exchanger, through the organic Rankine cycle energy conversion system, and back to the accumulation tank.
The method of claim 21.

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